A111D3 D7TA12

NATL INST OF STANDARDS & TECH R.I.C.

A1 11 0307981

Brennan, J. A/Effect of pipe roughness o QC100 .U5753 N0.1329 1989 V198 C.1 NISTC 5

NIST

PUBLICATJONS

NIST TECHNICAL NOTE 1329

U.S. DEPARTMENT OF COMMERCE /National Institute of Standards and Technology
rhcNational Institute of Standards and Technology1 was established by an act of Congress on March 3, 1901. The Institute's overall goal is to strengthen and advance the Nation's science and technology and

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'Headquarter* and Laboratories at Oaithersburg, MD, unless otherwise noted; mailing address Oaithersburg, MD 20899. 'Some divisions within the center are located at Boulder, CO 80303.

' Located at Boulder, CO, with some elements at Oaithersburg, MD.
Effect of Pipe Roughness vb. b>?

on Orifice Flow Measurement '?**

J. A. Brennan

S. E. McFaddin

C. F. Sindt

R. R. Wilson

Chemical Engineering Science Division

Center for Chemical Engineering

National Engineering Laboratory

National Institute of Standards and Technology

Boulder, Colorado 80303-3328

^

of c0a / w \

c

^£FJ ^j

St*tEs o* *

U.S. DEPARTMENT OF COMMERCE, Robert A. Mosbacher, Secretary

NATIONAL INSTITUTE OF STANDARDS AND TECHNOLOGY, Raymond G. Kammer, Acting Director

Issued July 1989
National Institute of Standards and Technology Technical Note 1329

Natl. Inst. Stand. Technol., Tech Note 1329, 66 pages (Jul. 1989)

CODEN:NTNOEF

U.S. GOVERNMENT PRINTING OFFICE

WASHINGTON: 1989

For sale by the Superintendent of Documents, U.S. Government Printing Office, Washington, D.C. 20402-9325
Table of Contents

Page

Acknowledgements , iv

List of Figures v

List of Tables vi

Abstract 1

Introduction 1

Literature Review 2

Surface Finish Measurement 5

Test Results and Discussion 6

Conclusions 9

Recommendations 9

References 11

Appendix

Measured and Calculated Quantities in SI Units for the

Upstream Pipe Roughness Study 25
Acknowledgements

The work described in this report was funded by the Gas Research Institute, Chicago,

Illinois, under GRI Contract No. 5081-353-0422 and 5088-271-1680. Kiran M. Kothari is the

project manager and his technical support for this effort is gratefully acknowledged. We

would also like to acknowledge the cooperation and helpful suggestions provided by James R. Whetstone of NIST in Gaithersburg, Maryland during the formative stages of this project, and

the support and technical guidance of the Basic Gas Metering Research Steering Committee.

Finally, the assistance received from the other laboratories, NIST-Gaithersburg and Colorado

Engineering Experiment Station, Inc., in running some of the tests is also acknowledged.

IV
List of Figures

Page

Figure 1. Effect of rusty pipe on the orifice discharge coefficient with a 0.75 12 beta ratio plate in a 250 mm orifice meter [12].

Figure 2. Surface finish representation. 13

Figure 3. Orifice meter schematic. 14

Figure 4. Discharge coefficient vs. Reynolds no. in water and nitrogen gas for a 15

beta ratio of 0.65 in a 3- in meter tube with an upstream pipe roughness

of 0.89 Aim (35 pin) .

Figure 5. Discharge coefficient vs. Reynolds no. in water and nitrogen gas for a 15 beta ratio of 0.65 in a 3 -in meter tube with an upstream pipe roughness

of 4.1 pm (160 pin).

Figure 6. Discharge coefficient vs. Reynolds no. in water and nitrogen gas for a 16 beta ratio of 0.65 in a 3- in meter tube with an upstream pipe roughness

of 7.6 pm (300 pin)

Figure 7. Discharge coefficient vs. Reynolds no. in nitrogen gas for a beta ratio 16 of 0.49 in a 3-in meter tube with upstream pipe roughnesses of 0.89,

4.1 and 7.6 pm (35, 160, and 300 pin).

Figure 8. Discharge coefficient vs. Reynolds no. in water and nitrogen gas for a 17 beta ratio of 0.57 in a 3-in meter tube with upstream pipe roughnesses

of 0.89, 4.1 and 7.6 pm (35, 160, and 300 pin).

Figure 9. Discharge coefficient vs. Reynolds no. in water and nitrogen gas for a 17 beta ratio of 0.65 in a 3-in meter tube with upstream pipe roughnesses

of 0.89, 4.1, and 7.6 mm (35, 160, and 300 pin).

Figure 10. Discharge coefficient vs. Reynolds no. in water and nitrogen gas for a 18 beta ratio of 0.73 in a 3-in meter tube with upstream pipe roughnesses

of 0.89, 4.1 and 7.6 pm (35, 160, and 300 pin).

Figure 11. Discharge coefficient vs. Reynolds no. in nitrogen gas for a beta ratio 18 of 0.43 in a 4- in meter tube with upstream pipe roughnesses of 0.76,

3.8 and 6.9 pm (30, 150, and 270 pin).

Figure 12. Discharge coefficient vs. Reynolds no. in water and nitrogen gas for a 19 beta ratio of 0.55 in a 4- in meter tube with upstream pipe roughnesses

of 0.76, 3.8 and 6.9 pm (30, 150, and 270 pin).

Figure 13. Discharge coefficient vs. Reynolds no. in water and nitrogen gas for a 19

beta ratio of 0.67 in a 4- in meter tube with upstream roughnesses of

0.76, 3.8 and 6.9 pm (30, 150, and 270 pin).

Figure 14. Discharge coefficient vs. Reynolds no. in water and nitrogen gas for a 20

beta ratio of 0.73 in a 4- in meter tube with upstream roughnesses of

0.76, 3.8 and 6.9 pm (30, 150, and 270 pin).

Figure 15. Discharge coefficient vs. Reynolds no. in water for a beta ratio of 20

0.49 in a 6 -in meter tube with upstream pipe roughnesses of 2.8, 5.1

and 8.9 pm (110, 200, and 350 pin).

Figure 16. Discharge coefficient vs. Reynolds no. in air for a beta ratio of 0.57 21 in a 6 -in meter tube with upstream pipe roughnesses of 2 . 8 , 5.1 and 8.9

pm (110, 200, and 350 pin).

Figure 17. Discharge coefficient vs. Reynolds no. in water and air for a beta 21 ratio of 0.66 in a 6- in meter tube with upstream roughnesses of 2.8,

5.1 and 8.9 pm (110, 200, and 350 pin).
List of Figures (cont.)

Page

Figure 18. Discharge coefficient vs. Reynolds no. in water and air for a beta 22

ratio of 0.74 in a 6- in meter tube with upstream roughnesses of 2.8,

5.1 and 8.9 pm (110, 200, and 350 pin)

.

Figure 19. Discharge coefficient vs. Reynolds no. for 0.43 beta ratio in a 4- in 22

meter tube with an upstream rough pipe honed smooth for two pipe

diameters from the orifice plate.

Figure 20. Discharge coefficient vs. Reynolds no. for 0.55 beta ratio in a 4- in 23

meter tube with an upstream rough pipe honed smooth for two pipe

diameters from the orifice plate.

Figure 21. Discharge coefficient vs. Reynolds no. for 0.67 beta ratio in a 4- in 23

meter tube with an upstream rough pipe honed smooth for two and four

pipe diameters from the orifice plate.

Figure 22. Discharge coefficient vs. Reynolds no. for 0.73 beta ratio in a 4- in 24

meter tube with an upstream rough pipe honed smooth for two and four

pipe diameters from the orifice plate.

vi
List of Tables

Page

Table 1. Average observed changes in the discharge coefficient in a 2 -in orifice 3 meter attributable to pipe roughness [6].

Table 2. Measured roughness values for all the meter tubes used in this study. 6

Table 3. Orifice meter tube lengths. 6

Table 4. Summary of experimental results 8
Effect of Pipe Roughness on Orifice Flow Measurement

J. A. Brennan, C.F. Sindt, S.E. McFaddin, and R.R. Wilson

National Institute of Standards and Technology

Boulder, Colorado 80303
Effect of Pipe Roughness on Orifice Flow Measurement

J. A. Brennan, C.F. Sindt, S.E. McFaddin, and R.R. Wilson

National Institute of Standards and Technology

Boulder, Colorado 80303

Abstract

Flow measurement with orifice flowmeters is simple in concept and can be

accurate, but as has been demonstrated in flow measurement test facilities can also

result in large errors if any of the significant parameters are not controlled.

Many of these parameters are well known and particular care is taken to ensure that

they do not cause measurement errors. Others are more subtle and not so easily

detected or controlled. One such parameter is the surface finish of the pipe

immediately upstream of the orifice plate. Results of an experimental

investigation into the effects of this pipe- roughness on the orifice discharge

coefficient are presented, along with a review of some of the pertinent literature.

Measurement errors of approximately 1 percent can result from using meter tubes

that are too rough but still within the specification of the standards.

Key words: air; experimental; flow measurement; nitrogen gas; orifice discharge

coefficient; orifice meter; roughness; surface finish; water.

Introduction

In many experimental programs designed to determine discharge coefficients for orifice

flow measurements, several important parameters that affect the results have been identified.

One parameter is the surface finish or roughness of the pipe upstream of the orifice plate.

Both the U.S. [1] and ISO [2] standards on orifice flow measurement have tolerances for the

pipe roughness, but they are different from one another and neither adequately defines the

correct allowable roughness values for all permissible beta ratios (orifice diameter/pipe

diameter). Surface finish is not a simple parameter to quantify. For example, ten ways to define the surface texture are tabulated in the ANSI standard [3], and published reports do

not always state which roughness value is being used. Reference 3 lists only one method

under the United States. That method is the arithmetic average roughness symbolized by Ra

. The maximum peak-to-valley roughness, Rv , and the ten-point height method, Rz

, along with Ra , are listed under ISO. AA and CLA were formerly used to symbolize the arithmetic average and

are equivalent to the Ra values. RMS, or root-mean-square, roughness values are not commonly

used and, in fact, require more specialized measuring equipment than is normally available.

It is suspected' that many of the references to RMS values should be Ra values. The only time

they are equivalent is when the surface finish is sinusoidal. A more complete description of

surface finish terminology is included in a later section of this report.

During the past several years, many experimental programs have investigated orifice flow

measurement. Those programs were carried out in many different laboratories throughout the . world. There has been considerable duplication of effort in that work and also with similar

work that was completed many years ago. Some of the work has been affected by pipe roughness

and has required discarding large amounts of data. Many of the problems caused by roughness

that were, faced in earlier work are still being repeated today largely because the previously

obtained data were not reported, not reported clearly, or could not be quantified because of

a confounding effect from another parameter. There may be several reasons for the lack of

adequate reporting, but in an effort to prevent unintended duplication in the future an attempt is made in this report to summarize the findings of the previous work and report the

results of a recently completed experimental program designed to quantify the upstream pipe

roughness effect.

The experimental program was a National Institute of Standards and Technology (NIST)

project under sponsorship of the Gas Research Institute (GRI) to systematically investigate

the effects of upstream pipe roughness on the orifice discharge coefficient. In this program

water, air, and nitrogen gas were the test fluids and data were taken on three orifice meter

sizes: 3, 4, and 6 inch. Data were collected on four orifice beta ratios (ratio of orifice

to pipe diameter) and three upstream pipe sections for each meter size. Each upstream

section had a different surface finish. The data using water were obtained on the NIST water

flow facility in Gaithersburg, Maryland (NIST-G) . The data using air were taken on a commercial flow facility and the data using nitrogen gas were taken on the NIST facility in

Boulder, Colorado (NIST-B) [4].

1
Literature Review

This review is not intended to be all inclusive. Rather, its purpose is to indicate

that the surface roughness problem has been recognized for a long time and that there is a consistent pattern, within the literature, that clearly shows the surface roughness

specification in the flow measurement standards need some modification if flow measurement

errors are to be avoided.

McNulty and Spencer [5] carried out some roughness experiments with a 4- inch orifice

meter which also included a variation in the diameter of the orifice plate holder. This

caused a step change in the pipe diameter in close proximity to the orifice plate. The

experiments were carried out using three different pipes. They described one of their pipes

as "'rough,' i.e., the paint work on the inside of the pipe had broken down, exposing the

metal in parts." Another pipe "was machined for a length of approximately 6 diameters

upstream and downstream, and repainted with an anti-corrosion paint." The third pipe was "chromium-plated internally after honing and gave CLA readings of about 10 micro inches." No

roughness values were reported for the two non-honed pipes ; they were only referred to as rough and smooth. Four orifice plates with beta ratios of 0.4, 0.6, 0.74; and 0.8 were used.

The data reported in [5] are difficult to categorize with respect to roughness because

close to the orifice plate they had variable disturbances that were not duplicated in all the

different pipes. The authors concluded that the increase in coefficient caused by an increase in the orifice plate" carrier diameter "was not so marked when the upstream pipe was very smooth." The data in this report could not be separated sufficiently to yield a magnitude for a change in orifice discharge coefficient resulting from pipe roughness effects

alone.'

In the late 1950's, the American Gas Association (A.G.A.) sponsored a study of the

effect of pipe roughness on orifice meter accuracy. Experimental work was conducted with

water at the Naval Boiler and Turbine Laboratory and with natural gas at a natural gas

company. This study consisted of testing both 2- and 4-inch flowmeters [6,7]. Originally,

the 2 -inch tests were to include five meter tubes with varying degrees of roughness and five

orifice plates with beta ratios from 0.36 to 0.75 [6]. The first phase of the project was to use water as the test fluid and the second phase was to use natural gas.

After the first water test "...both tubes A and C had become rusted in varying degrees."

Therefore, the project had to be revised. The revised program consisted of only two meter

tubes and three beta ratio orifice plates (0.5, 0.6, and 0.75). One of the meter tubes was constructed of stainless steel to control the rusting and was honed to a surface finish of

1.3 nm (50 /jin) • This meter tube served as the "reference meter." The other tube was one of

the original meter tubes that had not been tested in water and had a surface finish of 10 pirn (400 £iin) . Special care was taken to control the rusting of this meter tube during the test

program. It is assumed that the reported roughness values were Ra values.

All tests were run at nearly the same flow rate which produced an orifice differential

pressure of approximately 22 kPa (90 in H2O) and pipe Reynolds numbers as shown in table 1. A very consistent correlation of increasing discharge coefficient with increasing beta ratio

and increasing pipe roughness was observed. Table 1 lists the averages of the observations

published in [6]. In the table, the symbol C represents the discharge coefficient and the

subscripts R and S refer to the rough and smooth pipes. Based on these results, the authors

recommended that additional tests be run with a 4- inch meter with beta ratios of 0.5 and 0.6.

HHM
Table 1 Average observed changes in the discharge coefficient

in a 2- inch orifice meter attributable to pipe roughness

Beta Test Pipe Reynolds CR- C S Ratio Fluid Number • 100

0.5 water 6.3x10" 0.1

0.5 gas 4.15xl05 0.1

0.6 water 9.3x10" 0.2

0.6 gas 6.24xl05 0.5

0.75 water 1.74xl0 5 0.5

0.75 gas 1.09xl06 1.0

Test results from the A.G.A. project using the 4-inch meters were also reported by Bean

and Murdock [7]. Five seamless meter tubes were used for these tests with one reserved as a reference meter and the other four used to provide variations in roughness. Using orifice

plates with beta ratios of 0.5 and 0.6, base data were obtained on all five meter tubes,

which were characterized as "normal mill surface."

Roughness was determined on the original 4- inch meter tubes by cutting a small section

out of the meter tube at the location where the orifice flanges were to be attached.

Measurements were made on this small section using a profilometer and the values ranged from

2.3 to 4.3 fim (90 to 170 /iin) for all five meter tubes. It is assumed that these roughness

values are the arithmetic average values, Ra.

After the base data tests were completed, two of the meter tubes were honed and

retested. The roughness of the honed tubes was measured but this time the measurements were

made on the actual meter tubes rather than a cut-out sample. The range of roughness varied

from 0.5 to 2.3 urn (20 to 130 fiin) for these honed tubes and the average of all the

measurements was 1.0 to 1.2 pm (41 to 47 /ii n ) •

This test program was carried out at a natural gas company using natural gas as the test

fluid. All tests were run at nearly the same flow rate which produced an orifice

differential pressure of approximately 22 kPa (90 in H2O) and pipe Reynolds numbers between 1 and 2xl0 6

. The authors reported that the "results conclusively indicated that tubes can be

honed without affecting their accuracy." As will be discussed in a later section of this

report, the range of beta ratios, roughness, and Reynolds numbers was probably not large

enough in these 4- inch tests to show the effect of roughness on the discharge coefficient.

Clark and Stephens [8] investigated the effect of roughness in 12-, 6-, and 3- inch pipes

using air, and in a 3-inch pipe using water. Four orifice beta ratios were used ranging from

0.50 to 0.71. They produced different values of roughness by lining the pipes. The linings

included wallpaper, sand particles, dried peas, and glass spheres. The length of the rough

section was generally 12 diameters and always left a narrow (1.3-1.9 cm (1/2-3/4 in)) strip

of smooth pipe next to the orifice plate. This method of producing roughness simulated very

rough pipe.

Results from these tests are presented as combined roughness and pipe diameter change;

that is, pipe diameters were measured before adding the rough linings. Differences in

discharge coefficients of several percent were measured for all pipe sizes. The observed

differences are much larger than have been reported by any other known source.

Downstream pipe roughness was also studied by Clark and Stevens and found to be

insignificant compared to the upstream pipe roughness effect. Cleaning of the upstream pipe

was also investigated for all pipe sizes and the stated conclusion was "...that cleaning a rough upstream pipe adjacent to an orifice plate for a relatively short distance reduces

errors which may be otherwise very considerable to within known small limits." A table given

in the report lists recommended upstream clean pipe requirements to get roughness errors not

exceeding a stated value. Since the results reported in this paper are rather unique (that

is, the results are confounded by the change in pipe diameter; thus the errors are very large
and the effect of roughness not easily separated) , the reader is referred to the original

paper for further information.

A three- facility interlaboratory test of a 200 mm orifice meter that included an investigation of the effect of pipe roughness was reported by Spencer, Calame, and Singer

[9]. These tests were all run with water as the test fluid and conclusively showed that the

discharge coefficient for a 0.8 beta ratio plate increased by 1.6% in rough pipe compared to smooth pipe at a Reynolds number of 1.2xl06

. Included in these tests was a systematic

elimination of other possible causes of the difference in the discharge coefficient.

Two values of roughness were included in the tests reported in [9]. One, referred to as rough, was actually a commercial pipe; the other was a pipe specially selected for roundness

and smoothness. A friction factor was determined by measuring pressure drop over a length of

pipe, and then a relative roughness was calculated. The value thus calculated for the

"rough" pipe was such that it would be "...classed as a relatively smooth pipe." Similar

measurements were made on the smooth pipe, and it was "...significantly smoother than..." the

rough pipe. The actual values of friction factor for the two pipes were given as 0.018 for

the rough and 0.011 for the smooth pipe.

Reader-Harris and Keegans [10] have included pipe roughness as a parameter in their

computational work and have compared computed discharge coefficients with some experimentally

determined values. In general, the comparisons are quite good and show a significant

roughness effect. In addition, they stated a belief that the experimentally determined

dependence of the discharge coefficient on Reynolds number to the -0.75 power is caused by

"...using pipes that are insufficiently smooth."

Sheikholeslami and Patel [11] have modeled flow through an orifice meter and have

included roughness as one of the parameters. At a pipe Reynolds number of 4xl06

, they

calculated an increase in discharge coefficient of 0.66% for an orifice beta ratio of 0.4 in an 8-inch flowmeter when the relative roughness was increased from 0.000 01 to 0.0001. They

found no experimental data that matched their range of variables. An additional computation

was made using a beta ratio of 0.6, a pipe Reynolds number of 106

, and a relative roughness

of 0.005 for which they did have some experimental data. In that case the computed increase

in discharge coefficient was about 0.9% and the experimental value was 1%. Their model shows

that the rough pipe decreases the upstream pressure and thereby reduces the orifice pressure

drop and causes the discharge coefficient to increase.

In an EEC orifice meter project in which a 100 and a 250 mm orifice meter were tested in

a number of flow facilities in Europe there was at least one case when the 250 mm pipe became

rusty [12]. Tests were run at a water flow facility on the pipe in the rusty condition and

then cleaned and tested again. Figure 1 is a plot of the data from [12] and clearly shows

the difference between those two tests. At the maximum Reynolds number, the difference in

the discharge coefficient exceeds 1%. Unfortunately, there was no indication of surface

finish given for either the rusty or the clean pipe.

One part of a previous (1985) GRI/NIST flow measurement project involved determining the

comparisons of the data obtained in nitrogen gas taken at NIST-B and in water taken at NISTG. A 3-inch carbon steel orifice meter was tested in both locations with either 5 or 6 different beta ratio orifice plates. At beta ratios less than 0.57 the comparisons were

quite good, but with increasing beta ratios the agreement got progressively worse, and the

water discharge coefficient was larger than that determined with nitrogen gas.

A second 3- inch orifice meter was constructed of stainless steel and was also tested in

water at NIST-G. The discharge coefficients determined with this flowmeter compared quite

well with those determined with the carbon steel meter tube, except for beta ratios of 0.57

and larger. As the beta ratio increased, the difference between the results from the two

meter tubes increased. At the largest Reynolds number, with the 0.73 beta ratio plate, the

difference between the discharge coefficients exceeded 1%. Again, the carbon steel discharge

coefficients were larger. The effect observed in these tests was reported for three orifice

plates (beta = 0.37, 0.65, and 0.73) in [13], and clearly showed that there was a roughness

effect for the two larger beta ratio plates.

The cause of the differences observed in those tests was a difference in roughness in

the meter tubes. Between the time the carbon steel meter tube was tested in Boulder and

Gaithersburg it had become very rusty. No roughness values are available for the rusty pipe,

but a visual inspection revealed that it had become quite rough. The stainless steel meter

tube, on the other hand, had an Ra surface finish of 2.3 pm (90 jiin) .
All of the test results listed above are consistent in the sense that they reported an increase in discharge coefficient with increased pipe roughness for large beta ratio orifice

plates. There are some inconsistencies in the reporting and the measurement of the surface

finishes, however. Since surface roughness can be such an important parameter, and its

measurement not a trivial procedure, some of the measurement techniques are described in the

next section.

Surface Finish Measurement

Conceptually, one of the simplest methods used for quantifying surface finish is the

comparative technique. In this method, surfaces of known roughness are successively visually

compared to the unknown surface and by a process of elimination an estimate is made of the

unknown roughness. Comparisons can be difficult because a surface's preparation has a large

effect on its appearance. The method is subjective and consequently operator dependent,

which makes the results unreliable.

Another method of roughness determination calculates the relative roughness, k/D , from

pressure drop measurements over a relatively long pipe. First, the friction factor must be

calculated from equation (1) and then the relative roughness can be calculated using the

Colbrook [14] equation (2). This method gives some average value of roughness over the

length of the pipe.

1 A

= -21og

A - (D2Ap)/(Lpv2

) (1)

k 2.51 +

3.7D R^/X .

(2)

where

X = friction factor

D = pipe diameter

Ap = pressure drop

L = pipe length

p = fluid density v = average fluid velocity

Rn = pipe Reynolds number

k = equivalent roughness

Relatively short pipes upstream of the orifice plate control the major portion of the

roughness effect, therefore, this averaging method could be unsuitable for nonuniformly rough

pipe.

A third method of determination is to measure the roughness directly. A variety of

instruments are available for making such measurements, both in a laboratory and in the

field. Using this method of roughness determination gives a more localized value, but making

measurements very far from the pipe ends can be difficult, especially in small pipes. Using

this method, it is possible to obtain different roughness values from a single pipe and,

thereby, better define the localized and perhaps the controlling surface.

No matter what measurement method is used, it is imperative that the values determined

be presented unambiguously. Since surface finish can be specified in different ways, a description of the method used should be stated. The method used for the tests reported in

the following sections of this report was the direct measurement with an instrument that gave

either the common Ra value or the Rz (ten-point height) value. These measurements are made

by moving a stylus over the surface to be measured; the instrument then proportions the areas

of the peaks and the valleys and establishes a center line such that the positive areas and

the negative areas are equal. It then determines the deviation from the center line. The

absolute value of the deviations are added and the average of these deviations is given as Ra

. This value is the absolute mean deviation, not the root-mean- square value, and appears

to be the value referred to in ANSI/API 2530 [1]. The surface roughness used in the Moody

[15] chart to determine relative roughness of pipes for pressure loss calculations is the

average of the valley bottoms to the peak tops (peak-to-valley) over the measured sample

length and appears to be the value referred to in ISO 5167 [2]. Figure 2 shows a pictorial

representation of the three surface finishes symbolized as Ra , Ry, and Rz

.
Ail roughness values listed on figures 3-21 and the tables in the appendix are Ra values. In table 2 both Ra and Rz values are given but all other references to roughness

measurements in the experimental portion of this report refer only to Ra values.

Another parameter, cut-off length, is also required to define the surface finish

measurement. The cut-off length is the length of the trace used to determine the center line

and the calculated area. The shorter the cut-off, the more likely that the finish value will

exclude longer irregularities, such as a long wave or surface curvature. The cut-off used

for the surface finish measurements reported here was 2.5 mm (0.10 in). The instrument

averaged five cut-off lengths to establish each reading.

Table 2 Measured roughness values for all the

meter tubes used in this study

Meter

Size

Smooth Intermediate Rough

Ra Rz Ra Rz Ra Rz

in fjia /j in /jm /iin fXD /iin /JH jiin fjm /iin /m /iin

3

4

6

0.89

0.76

2.80

35

30

110

6.1

4.6

18.7

240

180

735

4.1

3.8

5.1

160

150

200

27.7

21.8

32.0

1090

860

1260

7.6

6.9

8.9

300

270

350

44.7

46.5

56.5

1760

1830

2225

Test Results and Discussion

The effects of upstream pipe roughness on the orifice discharge coefficient were investigated with water, air, and nitrogen gas as the test fluids. Data were taken in three

orifice meter sizes, 3, 4, and 6 inch. Four beta ratios and three upstream surface finishes were investigated with each meter size. The data using water were taken at the NIST-G water

flow facility. The data taken in air were taken at a commercial flow facility and the data

taken in nitrogen gas were taken at the NIST-B facility.

In the tests run at NIST-B and the commercial facility it was not possible to determine

the orifice discharge coefficient directly. All test results yield the product of the

discharge coefficient and the expansion factor. The expansion factor was calculated

according to ANSI/API 2530 [1] and used to calculate the discharge coefficient. In the water

facility at NIST-G this was not necessary because the expansion factor was equal to 1.

The orifice meters used for the test of surface finish effects were all constructed

similarly. They consisted of an approach section, an upstream section, and a downstream

section, as shown in figure 3. All meters were made of stainless steel so that the surface

would not deteriorate during the test program. They were all made with only flange tappings.

Table 3 lists the lengths of the meter sections.

Table 3 Orifice meter tube lengths

Meter

Size

Approach Upstream Downstream

cm in

L

D cm in

L

D cm in

L

D

3 in

4 in

6 in

266

355

531

105

140

209

34

34

34

67

116

136

26.4

45.7

53.6

9 11

9

136

167

228

53.7

65.7

89.8

1716

15
An oversized Sprenkle flow conditioner located at the upstream end of the approach

section removed any flow disturbances that may have been present. Each meter included three

upstream sections, each of different surface roughness. The surface roughness ranged from

0.76 to 8.9 fim (30 to 350 /tin). The surfaces were prepared by honing the entire length of

the upstream section. The primary pattern resulting from the honing was circular and was consistent throughout the length of the upstream section.

The surface roughness was measured with a profilometer at three radial locations 20 cm

(8 in) from the upstream end, 20 cm (8 in) upstream of the pressure tap and in the plane of

the pressure tap. The surface finishes determined for the upstream sections are given in

table 2.

The test plan for determining the effects of the meter tube roughness on the orifice

discharge coefficient was randomized to determine any day-to-day effects, as well as the

effects of changing orifice plates. Data for all the tests are tabulated in the appendix.

The 3- inch meter was tested with water at NIST-G and with nitrogen gas at NIST-B. The

tests using water were made with orifice plates of 0.57, 0.65, and 0.73 beta ratios. The

tests using nitrogen gas were made with orifice plates of 0.49, 0.57, 0.65, and 0.73 beta

ratios

Some typical results obtained with the 0.65 beta ratio plate in the 3 -inch meter are shown in figures 4, 5, and 6, where each point represents a single independent data point.

Figures 7 through 10 show a comparison of the mean of the orifice discharge coefficients for

the three surface finishes and four beta ratios. These comparison graphs show that the

orifice discharge coefficient increases with surface roughness and is dependent on Reynolds

number and beta ratio. In this 3-inch meter, the maximum observed increase in orifice

discharge coefficient caused by roughness is 1% at a beta ratio of 0.73 and a Reynolds number

of 2xl06. Only the 0.49 beta ratio plate was not affected by the pipe surface roughness.

The 4-inch meter was also tested with water at NIST-G and with nitrogen gas at NIST-B.

The tests using water were made with the orifice plates of 0.55, 0.67, and 0.73 beta ratios.

The tests using nitrogen gas were made with the orifice plates of 0.43, 0.55, 0.67, and 0.73

beta ratios.

A comparison of the changes in the orifice discharge coefficient in the three surface

finishes and the four beta ratios are shown in figures 11 through 14. Each data point on these figures represents the average of the orifice discharge coefficient and the Reynolds

number at approximately the same Reynolds numbers. As with the 3-inch meter data, the graphs

show a trend of increasing orifice discharge coefficient as the surface roughness, Reynolds

number, and beta ratio increase. The change in the orifice discharge coefficient caused by

roughness is 1% at a beta ratio of 0.73 and a Reynolds number of 1.7xl06

. Only the 0.43 beta

ratio plate was not affected by the pipe roughness.

The 6- inch meter was tested with water at NIST-G and with air at a commercial flow

facility. The tests with water used orifice plates with the beta ratios of 0.49, 0.66, and

0.74. The test with air used orifice plates with beta ratios of 0.57, 0.66, and 0.74.

Comparisons of the change in orifice discharge coefficients are presented in figures 15 through 18. Each data point on these graphs represents the average of the orifice discharge

coefficient and the Reynolds number at approximately the same Reynolds numbers. The trends

of the data are the same as with the 3- and 4- inch meters; however, for the 6 -inch meter, the

data cover a much higher Reynolds number range and the change in discharge coefficient

continues to show an increase, especially at a beta ratio of 0.74. The change is 1.5%

between the surface finish of 2.8 /im (110 /iin) and 8.9 fim (350 /iin) at the maximum Reynolds

number. Only the 0.49 beta ratio plate was not affected by the pipe roughness.

Two data sets were omitted from the graphs, one set in the 4- inch data identified as 45051387-1 through -9 (table 36) and one set in the 3-inch data identified as 34042987-1

through -9 (table 5) . Neither of these sets of data fits the other data sets run at the same conditions nor do they fit the data trends of other data sets. No cause for the differences

was identified but it can be speculated that it was a badly positioned plate. The data are included in the tables in case they represent an anomaly of some real but unexplained cause.

The data show good agreement among the three laboratories. The 6-inch water and air

data match reasonably well where they meet. Also, the 4- inch water data match with the
gaseous nitrogen data where they meet. The largest mismatch between the water data and the

gas data is with the 0.65 beta ratio plate in the 3 -inch meter where the difference is

approximately 0.4%. The interlaboratory agreement is especially significant since the data

meet where the differential pressure across the orifice plate may be as much as 185 kPa (750

in H2O) in water and as little as 2.5 kPa (10 in H2O) in the gases.

These test results indicate that for beta ratios of 0.55 or larger, the current

specifications of surface roughness in the standards [1,2] are inadequate to assure that the

orifice discharge coefficient stays within the specified tolerance.

A summary of the experimental test results is given in table 4. The change in discharge

coefficient that is shown may not represent the maximum effect; It may have been larger at

higher Reynolds numbers. Even at the Reynolds numbers presented here, however, the magnitude

of the change clearly shows that control of the roughness is necessary to ensure accurate

flow measurement. In the table the symbol C represents the discharge coefficient and the

subscripts R, I, and S refer to the rough, intermediate, and smooth pipe.

Table 4

Summary of experimental results

Meter Beta Test Pipe Reynolds Cj-Cs CR" C S Size Ratio Fluid Number •

1 11 nnuu • 100

(in) c s c s

3 0.49 N2 gas 1.4xl06 <0.1 0.1

3 0.57 water 3.9xl05 <0.1 <0.1

3 0.57 N2 gas 1.8xl06 0.4 0.6

3 0.65 water 5.3xl05 <0.1 0.2

3 0.65 N2 gas 2.0xl06 0.4 0.8

3 0.73 water 7.0xl05 <0.1 0.3

3 0.73 N2 gas 2.1xl06 <0.1 1.0

4 0.43 N2 gas 1.3xl06 <0.1 <0.1

4 0.55 water 4.7xl05 <0.1 0.1

4 0.55 N2 gas 1.6xl06 0.2 0.4

4 0.67 water 7.5xl05 0.1 0.4

4 0.67 N2 gas 1.6xl06 0.3 0.5

4 0.73 water 9.4xl05 0.2 0.5

4 0.73 N2 gas 1.7xl06 0.2 1.0

6 0.49 water 4.5xl05 <0.1 <0.1

6 0.57 air 7.0xl06 0.2 0.5

6 0.66 water l.OxlO6 0.1 0.4

6 0.66 air 11.8xl06 0.2 1.0

6 0.74 water 1.4xl06 0.1 0.8

6 0.74 air 12.3xl06 0.3 1.5

An experimental study of the required upstream length of smooth pipe to eliminate the

roughness effects was also included in this program. This study used the 4- inch flowmeter

and consisted of honing the roughest upstream pipe section to an Ra surface finish of 1.3 /xm (50 /iin) , first two and then four diameters upstream of the orifice plate flange face.

The first tests, with the upstream section honed two pipe diameters upstream from the

orifice plate flange face, were run with orifice beta ratios of 0.43, 0.55, 0.67, and 0.73.

The data from these tests are plotted in figures 19 through 22. As expected, there was no

8
difference in the orifice coefficients for the 0.43 beta ratio plate and only a small effect

for the 0.55 beta ratio plate. For beta ratios of 0.67 and 0.73, the orifice coefficient

change was inconsistent. The results with the 0.67 beta ratio plate were nearly the same as when the upstream section was all rough and the results with the 0.73 beta ratio plate

changed significantly. In fact, the 0.73 beta ratio coefficient almost equals the value

obtained with the smooth pipe.

The upstream section was then honed for four pipe diameters upstream of the orifice

plate flange. Tests were run with the 0.67 and the 0.73 beta ratio plates. These data are included in figures 21 and 22. There was no change between these results and the results

obtained when the pipe was only honed for two pipe diameters , nor were the coefficients the same as with the smooth pipe.

The figures show the data obtained with the pipe honed for both two and four pipe

diameters upstream from the orifice plate. Data with the smooth upstream section and the

rough upstream section are also shown and are indicated by the solid and dashed lines,

respectively. The first impression is that the rough upstream meter tube may just result in

different orifice coefficients even if it were honed for its entire length. However, the

data for beta ratios of 0.43 and 0.55, which are shown in figures 19 and 20, indicate that

the data are the same for the two meter tubes. These results show that more than four pipe

diameters of smooth pipe are required to control the discharge coefficient.

Conclusions

A consistent pattern in both the published literature and in the new experimental data

shows that the effect of upstream pipe roughness on the orifice discharge coefficient is

related to the pipe's surface finish, the orifice beta ratio, and the pipe Reynolds number.

The largest change in discharge coefficient occurs at the highest beta ratio and the largest

Reynolds numbers. The published literature does not give enough information to indicate the

overall relationships, but the trends are consistent with the new experimental data. With

the new data it is possible to draw some definite conclusions about the effect of roughness

on meter sizes through 6 inches, and figure 1 shows that the effect is also present in 10-

inch flowmeters.

The following conclusions are drawn from the new experimental data generated in this

program. These conclusions are based on the range of parameters tested and may require

modification at other values of the parameters. For example, the change in discharge

coefficient may be larger at higher Reynolds numbers.

1. For orifice beta ratios less than 0.5, there is no statistically significant effect

on the discharge coefficient caused by roughness within the present ANSI/API 2530

specification [1].

2. For Ra roughness values less than 3.8 jxm (150 /xin) the effect on the discharge

coefficient caused by roughness is less than 0.5% for any beta ratio less than 0.75.

3. For orifice beta ratios > 0.55 and Ra roughness values > 3.8 /im (150 ^in) , a statistically significant roughness effect on the discharge coefficient does exist.

4. For an orifice beta ratio of 0.73 and an approximate Ra roughness value of 7.6 /im (300 A*in) the roughness effect on the discharge coefficient can exceed 1%.

5. The surface finish tolerance in both standards [1,2] is not adequate to prevent flow

measurement errors that can exceed 1%.

6. Honing the orifice meter for two or four pipe diameters upstream of the orifice plate

to a roughness of 1.3 fim (50 pin) will not remove all of the effects of upstream pipe

roughness apparent with beta ratios of 0.67 and higher.

Recommendations

Based on the findings in the experimental program and a review of the published

literature, the following recommendations are suggested as necessary changes to the existing

orifice meter standards.

1. Orifice beta ratios should not exceed 0.5 for flow measurement installations in which

the pipe roughness of the upstream pipe is not known.
2. The arithmetic average roughness, Ra , should not exceed 3.8-5.1 fim (150-200 /iin) if

orifice beta ratios larger than 0.55 will be used.

3. Roughness tolerances should continue to be specified on an absolute, not a relative,

roughness basis.

At this time, the required length of smooth upstream pipe is not defined well enough to make a recommendation in this area. The experimental results with the 4- inch meter show that

four diameters or less are not sufficient for returning the meter to the equivalent of a long

smooth upstream section for all beta ratios. Four diameters does appear sufficient for all

but the largest tested beta ratios. Additional work in this area needs to be completed

before definitive recommendations can be made.

10
References

1. Orifice metering of natural gas and other related hydrocarbon fluids, A.G.A. Report No.

3- -ANSI/API 2530, Second Edition, American Gas Association, Arlington, VA 22209

(September 1985)

2. Measurement of fluid flow by means of orifice plates, nozzles and venturi tubes inserted

in circular cross-section conduits running full, International Standard ISO 5167, First

Edition, International Organization for Standardization (1980).

3. Surface texture (surface roughness, waviness, and lay), ANSI/ASME B46.1- 1985, The

American Society of Mechanical Engineers, New York, NY 10017, 43pp (1985).

4. McFaddin, S.E., J. A. Brennan, and C.F. Sindt, The precision and accuracy of mass flow

measurement in the NIST-Boulder nitrogen flow facility, Proceedings of the International

Conference on Mass Flow Measurement Direct and Indirect, London (Feb. 21-22, 1989).

5. McNulty, P.J. and E.A. Spencer, Tests on orifice plates in a 4-in. diameter pipe (effect

of pipe roughness and carrier diameter), MERL Fluids Note No. 74, East Kilbride,

Glasgow, 12pp (1959)

6. Bean, H.S. and J.W. Murdock, Effect of pipe roughness on orifice meter accuracy, Report

of supervising committee on two- inch tests, American Gas Association Research Project

NW-20, American Gas Association, New York, NY (Jan. 1959).

7. Bean, H.S. and J.W. Murdock, Effect of pipe roughness on orifice meter accuracy, Report

of supervising committee on four inch tests, American Gas Association Research Project

NW-20, American Gas Association, New York, NY (Feb. 1960).

8. Clark, W.J. and R.C. Stephens, Flow measurement by square -edged orifice plates: pipe

roughness effects, Proc . Institution of Mech. Engrs . (London), 171 . n33, 895-910 (1957).

9. Spencer, E.A., H. Calame, and J. Singer, Edge sharpness and pipe roughness effects on orifice plate discharge coefficients, National Engineering Laboratory, UK, NEL Report

No. 427 (Aug. 1969).

10. Reader-Harris, M.J. and W. Keegans , Comparisons of computation and LDV measurement of

flow through orifice and perforated plates, and computation of the effect of rough

pipework on orifice plates, Proceedings International Symposium of Fluid Flow

Measurement, American Gas Association, Arlington, VA (Nov. 16-19, 1986).

11. Sheikholeslami , M.Z. and B.R. Patel, Numerical modeling of flow through orifice meters,

Topical Report from Creare Incorporated, Hanover, NH, to Gas Research Institute,

Chicago, IL (Mar. 1988)

12. Hobbs , J.M., J. A. Sattary, and A.D. Maxwell, Experimental data for the determination of

basic 250 mm orifice meter discharge coefficients, Commission of the European

Communities, BCR Information Applied Metrology, Report EUR 10979 (1987).

13. Brennan, J. A., B.R. Bateman, S.E. McManus , C.F. Sindt, and I. Vazquez, NBS-Boulder

basic gas metering project, Proceedings 1986 Operating Section, American Gas

Association, Arlington, VA (1986).

14. Colbrook, C.F., Turbulent flow in pipes, with particular reference to the transition

region between the smooth and rough pipe laws, J. Institution of Civil Engr. (Great

Britain), U, 133-156, Paper No. 5024 (1938-1939).

15. Moody, L.F., Friction factors for pipe flow, Trans. ASME, 66, 671-684 (1944).

11
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Pipe Reynolds Number/1 000 000

Figure 1. Effect of rusty pipe on the orifice discharge coefficient with a 0.75 beta ratio

plate in a 250 mm orifice meter [12].

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Figure 4. Discharge coefficient vs. Reynolds no. in water and nitrogen gas for a beta ratio

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Figure 6. Discharge coefficient vs. Reynolds no. in water and nitrogen gas for a beta ratio

of 0.65 in a 3 -in meter tube with an upstream pipe roughness of 7.6 fim (300 /iin) .

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Figure 7. Discharge coefficient vs. Reynolds no. in nitrogen gas for a beta ratio of 0.49

in a 3-in meter tube with upstream pipe roughnesses of 0.89, 4.1, and 7.6 /*m (35

160, and 300 fxin)

.

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,

Discharge coefficient vs. Reynolds no. in water and nitrogen gas for a beta ratio

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Figure 9. Discharge coefficient vs. Reynolds no. in water and nitrogen gas for a beta ratio

of 0.65 in a 3- in meter tube with upstream pipe roughnesses of 0.89, 4.1, and

7.6 mm (35, 160, and 300 pin).

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Figure 10. Discharge coefficient vs. Reynolds no. in water and nitrogen gas for a beta ratio

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7.6 urn (35, 160, and 300 /iin) .

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Figure 11. Discharge coefficient vs. Reynolds no. in nitrogen gas for a beta ratio of 0.43

in a 4- in meter tube with upstream pipe roughnesses of 0.76, 3.8, and 6 . 9 pm (30,

150, and 270 /iin) .

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and 350 pin)

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Figure 18. Discharge coefficient vs. Reynolds no. in water and air for a beta ratio of 0.74

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Pipe Reynolds Number/1 000 000

2.0

Figure 19. Discharge coefficient vs. Reynolds no. for 0.43 beta ratio in a 4- in meter tube

with an upstream rough pipe honed smooth for two pipe diameters from the orifice

plate.

22
0.63

Q

u

o

CDo

CJ

CD00

U

cj73

0.62

0.61

0.60

0.59

2 D Honed

0.76 nm Finish

1%

0.0 0.5 1.0

Pipe Reynolds Number,

1.5

1 000 000

2.0

Figure 20. Discharge coefficient vs. Reynolds no. for 0.55 beta ratio in a 4- in meter tube

with an upstream rough pipe honed smooth for two pipe diameters from the orifice

plate.

0.63

Q

c

CD

CJ

o

CJ

CDu

CC sz

CJ

73

0.62 -

0.61

0.60 -

0.59

— — - 6.9 /i.m Finish

4 D Honed

H 2D Honed

a

1%

0.5 1.0 1.5

Pipe Reynolds Number/1 000 000

2.0

Figure 21. Discharge coefficient vs. Reynolds no. for 0.67 beta ratio in a 4-in meter tube

with an upstream rough pipe honed smooth for two and four pipe diameters from the

orifice plate.

23
0.63

Q

u

c

• 1—

I

u

0.62

0)O 0.61

u

on

o

CO

0.60

0.59

6.9 fun Finish

4 D Honed

D 2D Honed

o^On o

i i

1%

0.5 1.0 1.5 2.0

Pipe Reynolds Number/l 000 000

Figure 22. Discharge coefficient vs. Reynolds no. for 0.73 beta ratio in a A- in meter tube

with an upstream rough pipe honed smooth for two and four pipe diameters from the

orifice plate.

24

;
APPENDIX

Measured and Calculated Quantities in SI Units for the Upstream Pipe Roughness Study

To convert from

psi

in. of water (60°F)

inch

inch

/xin

°R

lb/s

CONVERSION FACTORS

To

MPa

kPa

cmmm

fim K

kg/s

Multiply By

6.8948 x 10' 3 0.24884

2.54

25.4

0.0254

0.55556

0.45359

25
List of Tables

Page

Table 1. Measured and Calculated Quantities Using Nitrogen Gas in the 3-Inch 30

Orifice Meter, 0.49 Beta Ratio, 0.89 /im Roughness

Table 2. Measured and Calculated Quantities Using Nitrogen Gas in the 3-Inch 30

Orifice Meter, 0.49 Beta Ratio, 4.1 fim Roughness

Table 3. Measured and Calculated Quantities Using Nitrogen Gas in the 3-Inch 30

Orifice Meter, 0.49 Beta Ratio, 7 . 6 /im Roughness

Table 4. Measured and Calculated Quantities Using Water in the 3-Inch Orifice 31 Meter, 0.57 Beta Ratio, 0.89 /im Roughness

Table 5. Measured and Calculated Quantities Using Nitrogen Gas in the 3-Inch 32

Orifice Meter, 0.57 Beta Ratio, 0.89 /im Roughness

Table 6. Measured and Calculated Quantities Using Water in the 3-Inch Orifice 33

Meter, 0.57 Beta Ratio, 4.1 /im Roughness

Table 7. Measured and Calculated Quantities Using Nitrogen Gas in the 3-Inch 33

Orifice Meter, 0.57 Beta Ratio, 4.1 /im Roughness

Table 8. Measured and Calculated Quantities Using Water in the 3-Inch Orifice 33

Meter, 0.57 Beta Ratio, 7.6 /im Roughness

Table 9. Measured and Calculated Quantities Using Nitrogen Gas in the 3-Inch 34

Orifice Meter, 0.57 Beta Ratio, 7 . 6 /im Roughness

Table 10. Measured and Calculated Quantities Using Water in the 3-Inch Orifice 34

Meter, 0.65 Beta Ratio, 0.89 /im Roughness

Table 11. Measured and Calculated Quantities Using Nitrogen Gas in the 3-Inch 35

Orifice Meter, 0.65 Beta Ratio, 0.89 /im Roughness

Table 12. Measured and Calculated Quantities Using Water in the 3-Inch Orifice 35

Meter, 0.65 Beta Ratio, 4.1 /im Roughness

Table 13. Measured and Calculated Quantities Using Nitrogen Gas in the 3-Inch 36

Orifice Meter, 0.65 Beta Ratio, 4.1 /tm Roughness

Table 14. Measured and Calculated Quantities Using Water in the 3-Inch Orifice 36

Meter, 0.65 Beta Ratio, 7 . 6 /tm Roughness

Table 15. Measured and Calculated Quantities Using Nitrogen Gas in the 3-Inch 37

Orifice Meter, 0.65 Beta Ratio, 7 . 6 /im Roughness

Table 16. Measured and Calculated Quantities Using Water in the 3-Inch Orifice 37 Meter, 0.73 Beta Ratio, 0.89 /im Roughness

Table 17. Measured and Calculated Quantities Using Nitrogen Gas in the 3-Inch 38

Orifice Meter, 0.73 Beta Ratio, 0.89 /tm Roughness

Table 18. Measured and Calculated Quantities Using Water in the 3-Inch Orifice 38

Meter, 0.73 Beta Ratio, 4.1 /im Roughness

Table 19. Measured and Calculated Quantities Using Nitrogen Gas in the 3-Inch 39

Orifice Meter, 0.73 Beta Ratio, 4.1 /im Roughness

Table 20. Measured and Calculated Quantities Using Water in the 3-Inch Orifice 39

Meter, 0.73 Beta Ratio, 7 . 6 /im Roughness

Table 21. Measured and Calculated Quantities Using Nitrogen Gas in the 3-Inch 40

Orifice Meter, 0.73 Beta Ratio, 7 . 6 /im Roughness

Table 22. Measured and Calculated Quantities Using Nitrogen Gas in the 4-Inch 41

Orifice Meter, 0.43 Beta Ratio, 0.76 /im Roughness

26
List of Tables (cont.)

Page

Table 23. Measured and Calculated Quantities Using Nitrogen Gas in the 4-Inch 41

Orifice Meter, 0.43 Beta Ratio, 3 . 8 iim Roughness

Table 24. Measured and Calculated Quantities Using Nitrogen Gas in the 4-Inch 42

Orifice Meter, 0.43 Beta Ratio, 6 . 9 /xm Roughness

Table 25. Measured and Calculated Quantities Using Water in the 4-Inch Orifice 42

Meter, 0.55 Beta Ratio, 0.76 iim Roughness

Table 26. Measured and Calculated Quantities Using Nitrogen Gas in the 4-Inch 42

Orifice Meter, 0.55 Beta Ratio, 0.76 iim Roughness

Table 27. Measured and Calculated Quantities Using Water in the 4-Inch Orifice 43

Meter, 0.55 Beta Ratio, 3 . 8 /un Roughness

Table 28. Measured and Calculated Quantities Using Nitrogen Gas in the 4-Inch 43

Orifice Meter, 0.55 Beta Ratio, 3 . 8 iim Roughness

Table 29. Measured and Calculated Quantities Using Water in the 4- Inch Orifice 43

Meter, 0.55 Beta Ratio, 6 . 9 iim Roughness

Table 30. Measured and Calculated Quantities Using Nitrogen Gas in the 4- Inch 44

Orifice Meter, 0.55 Beta Ratio, 6.9 iim Roughness

Table 31. Measured and Calculated Quantities Using Water in the 4-Inch Orifice 44

Meter, 0.67 Beta Ratio, 0.76 iim Roughness

Table 32. Measured and Calculated Quantities Using Nitrogen Gas in the 4-Inch 44

Orifice Meter, 0.67 Beta Ratio, 0.76 iim Roughness

Table 33. Measured and Calculated Quantities Using Water in the 4-Inch Orifice 45

Meter, 0.67 Beta Ratio, 3 . 8 /im Roughness

Table 34. Measured and Calculated Quantities Using Nitrogen Gas in the 4-Inch 45

Orifice Meter, 0.67 Beta Ratio, 3 . 8 iim Roughness

Table 35. Measured and Calculated Quantities Using Water in the 4- Inch Orifice 45

Meter, 0.67 Beta Ratio, 6 . 9 fim Roughness

Table 36. Measured and Calculated Quantities Using Nitrogen Gas in the 4-Inch 46

Orifice Meter, 0.67 Beta Ratio, 6.9 ixni Roughness

Table 37. Measured and Calculated Quantities Using Water in the 4-Inch Orifice 46

Meter, 0.73 Beta Ratio, 0.76 iim Roughness

Table 38. Measured and Calculated Quantities Using Nitrogen Gas in the 4-Inch 47

Orifice Meter, 0.73 Beta Ratio, 0.76 iim Roughness

Table 39. Measured and Calculated Quantities Using Water in the 4-Inch Orifice 47

Meter, 0.73 Beta Ratio, 3 . 8 iim Roughness

Table 40. Measured and Calculated Quantities Using Nitrogen Gas in the 4- Inch 48

Orifice Meter, 0.73 Beta Ratio, 3 . 8 iim Roughness

Table 41. Measured and Calculated Quantities Using Water in the 4-Inch Orifice 48

Meter, 0.73 Beta Ratio, 6.9 iim Roughness

Table 42. Measured and Calculated Quantities Using Nitrogen Gas in the 4-Inch 48

Orifice Meter, 0.73 Beta Ratio, 6 . 9 iim Roughness

Table 43. Measured and Calculated Quantities Using Water in the 6-Inch Orifice 49

Meter, 0.49 Beta Ratio, 2 . 8 iim Roughness

27
List of Tables (cont.)

Table 44. Measured and Calculated Quantities Using Water in the 6-Inch Orifice

Meter, 0.49 Beta Ratio, 5.1 /im Roughness

Table 45. Measured and Calculated Quantities Using Water in the 6-Inch Orifice

Meter, 0.49 Beta Ratio, 8 . 9 /im Roughness

Table 46. Measured and Calculated Quantities Using Air in the 6-Inch Orifice

Meter, 0.57 Beta Ratio, 2 . 8 /im Roughness

Table 47. Measured and Calculated Quantities Using Air in the 6-Inch Orifice

Meter, 0.57 Beta Ratio, 5.1 /im Roughness

Table 48. Measured and Calculated Quantities Using Air in the 6-Inch Orifice

Meter, 0.57 Beta Ratio, 8 . 9 /im Roughness

Table 49. Measured and Calculated Quantities Using Water in the 6-Inch Orifice

Meter, 0.66 Beta Ratio, 2.8 /im Roughness

Table 50. Measured and Calculated Quantities Using Air in the 6-Inch Orifice

Meter, 0.66 Beta Ratio, 2.8 /mi Roughness

Table 51. Measured and Calculated Quantities Using Water in the 6-Inch Orifice

Meter, 0.66 Beta Ratio, 5.1 /im Roughness

Table 52. Measured and Calculated Quantities Using Air in the 6-Inch Orifice

Meter, 0.66 Beta Ratio, 5.1 /im Roughness

Table 53. Measured and Calculated Quantities Using Water in the 6-Inch Orifice

Meter, 0.66 Beta Ratio, 8 . 9 /im Roughness

Table 54. Measured and Calculated Quantities Using Air in the 6- Inch Orifice

Meter, 0.66 Beta Ratio, 8 . 9 /im Roughness

Table 55. Measured and Calculated Quantities Using Water in the 6-Inch Orifice

Meter, 0.74 Beta Ratio, 2.8 /im Roughness

Table 56. Measured and Calculated Quantities Using Air in the 6-Inch Orifice

Meter, 0.74 Beta Ratio, 2 . 8 /im Roughness

Table 57. Measured and Calculated Quantities Using Water in the 6-Inch Orifice

Meter, 0.74 Beta Ratio, 5.1 /im Roughness

Table 58. Measured and Calculated Quantities Using Air in the 6-Inch Orifice

Meter, 0.74 Beta Ratio, 5.1 /im Roughness

Table 59. Measured and Calculated Quantities Using Water in the 6-Inch Orifice

Meter, 0.74 Beta Ratio, 8.9 /im Roughness

Table 60. Measured and Calculated Quantities Using Air in the 6-Inch Orifice

Meter, 0.74 Beta Ratio, 8 . 9 /im Roughness

Table 61. Measured and Calculated Quantities Using Nitrogen Gas in the 4-Inch

Orifice Meter, 0.43 Beta Ratio, 6.9 /im Roughness Honed to 1.3 /im Roughness for Two Pipe Diameters

Table 62. Measured and Calculated Quantities Using Nitrogen Gas in the 4-Inch

Orifice Meter, 0.55 Beta Ratio, 6 . 9 /im Roughness Honed to 1.3 /im Roughness for Two Pipe Diameters

Table 63. Measured and Calculated Quantities Using Nitrogen Gas in the 4-Inch

Orifice Meter, 0.67 Beta Ratio, 6 . 9 /im Roughness Honed to 1.3 fim Roughness for Two Pipe Diameters

Page

49

49

50

50

50

50

51

51

51

51

52

52

52

53

53

53

53

54

54

54

28

MH
List of Tables (cont.)

Page

Table 64. Measured and Calculated Quantities Using Nitrogen Gas in the 4-Inch 54

Orifice Meter, 0.73 Beta Ratio, 6.9 pm Roughness Honed to 1.3 /jm

Roughness for Two Pipe Diameters

Table 65. Measured and Calculated Quantities Using Nitrogen Gas in the 4-Inch 55

Orifice Meter, 0.67 Beta Ratio, 6.9 pm Roughness Honed to 1.3 pm

Roughness for Four Pipe Diameters

Table 66. Measured and Calculated Quantities Using Nitrogen Gas in the 4- Inch 55

Orifice Meter, 0.73 Beta Ratio, 6.9 pm Roughness Honed to 1.3 pm

Roughness for Four Pipe Diameters

29
Table 1. Measured and Calculated Quantities Using Ritrogen Gas in the 3-Inch Orifice Meter, 0.49 Beta Ratio, 0.89 foa Roughness

Run ID

33042787- 1 33042787- 2 33042787- 3 33042787- 4 33042787- 5 33042787- 6 33042787- 7 33042787- 8 33102287- 1 33102287- 2 33102287- 3 33102287- 4 33102287- 5 33102287- 2 33102287- 3 33102287- 4

Pipe Diameter 7.816 cm Orifice Diameter 3.8087 cm

Pressure Temperature Density

(kg/m3

) Dif Press Flow Rate Pipe c C5f 2 (MPa) (K) (kPa) (kg/s) Reynolds No.

4 .0053 288.49 47.13 22.286 1.0287 923100 6046 0.6053

4 .0034 288.78 47.05 22.286 1.0315 925000 6067 0.6074 4.0991 289.51 48.05 6.174 0.5483 490200 6070 0.6072

4.1137 289.54 48.22 6.260 0.5522 493700 6062 0.6064 3.8909 289.77 45.56 49.487 1.5084 1351300 6041 0.6057 3.9102 289.27 45.87 49.237 1.5086 1352700 6037 0.6053 3.9845 289.53 46.70 31.614 1.2217 1093900 6053 0.6063 3.9923 290.07 46.69 31.807 1.2240 1094400 6046 0.6056 3.9630 286.28 47 .03 29. 795 1.1940 1077600 6073 0.6083 3.9568 288.09 46.63 29.755 1.1839 1063900 6051 0.6061 3.9558 287.82 46.66 29.628 1.1806 1061600 6045 0.6054 3.8929 288.94 45.72 49.503 1.5088 1354100 6031 0.6047 3.8795 288. 53 45.64 49.486 1.5064 1353400 6028 0.6044 4.0557 286.49 48.09 16.900 0.9059 816200 6054 0.6060

4. 1244 288.28 48.57 7.304 0.6012 538900 6086 0.6088 4.1351 287.66 48. 82 7.032 0.5894 529100 6066 0.6069

Table 2. Measured and Calculated Quantities Using Ritrogen Gas in the 3 -Inch Orifice Meter, 0.49 Beta Ratio, 4 . 1 iim Roughness

Run ID

33031087- 1 33031087- 2 33031087- 3 33031087- 4 33031087- 5 33031087- 6 33041687- 1 33041687- 2 33041687- 3 33041687- 4 33041687- 5 33041687- 7 33041687- 8 33041687- 9 33110987- 1 33110987- 2 33110987- 3 33110987- 4 33110987- 5 33110987- 6 33110987- 7 33110987- 8

Table 3.

Pipe Diameter » 7.813 cm Orifice Diameter 3.8087 cm

Pressure Temperature Density

(kg/m 3

) Dif Press Flow Rate Pipe c CY 2 (MPa) (K) (kPa) (kg/s) Reynolds No. 3.9191 287.46 46.29 48.302 1.5021 1352900 6042 . 6057 3.9202 287 .48 46.30 48.155 1.5000 1350800 6042 0.6057

4 .0575 288.33 47 . 78 23 .693 1.0705 960500 6060 0.6067 4.0524 287 .87 47.80 23.754 1.0718 962800 6058 0.6066

4 . 1180 288.83 48.40 6.714 0.5742 514200 6075 0.6077

4 . 1309 288.92 48. 53 6.003 0.5431 486200 6069 0.6071 3.8723 287.99 45.65 49.616 1.5101 1359000 6035 0.6051

3.8724 288.35 45.59 49.664 1.5102 1358000 6036 0.6052

4 . 1060 289.30 48. 17 6.918 0.5807 519500 6065 0.6068

4. 1013 289.33 48.11 7.147 0.5897 527600 6064 0.6066 3.9976 287.36 47.24 29.985 1.1949 1075400 6045 0.6054

4 .0088 288. 13 47 .24 29.749 1.1919 1070500 6054 0.6063

4 .0818 288.61 48.01 16.632 0.8988 805700 6060 0.6065

4.0714 288.90 47.83 16.636 0.8972 803700 6059 0.6065

3. 9464 287.62 46.59 31.135 1.2089 1088100 6043 .6053 3.9346 287 .68 46 . 44 30.853 1. 1969 1077300 6020 0.6030

4 .0388 288. 12 47.59 18. 105 0.9320 836900 6048 0.6054

4 .0405 288.21 47 .60 18.159 0.9342 838600 6054 0.6059 3.8918 287.59 45.95 48.152 1.4895 1341500 6023 0.6038 3.8769 287.75 45.74 48.788 1.4940 1345300 6015 0.6030 4.1191 289.14 48.35 8.303 0.6377 570600 6066 0.6069

4 . 1580 289. 17 48. 80 8.574 0.6505 581800 6062 0.6064

Measured and Calculated Quantities Using Ritrogen Gas in the 3-Inch Orifice Meter, 0.49 Beta Ratio, 7.6 am Roughness

Pipe Di ameter 7.811 cm Orifice Diameter TM 3.8087 cm

Run ID Pressure Temperature Density

(kg/m 3

) Dif Press Flow Rate Pipe c CY 2 (MPa) (K) (kPa) (kg/s) Reynolds No 33031287- 1 3.9127 287.62 46.19 49.727 1.5287 1377000 6066 0.6082 33031287- 2 3.9135 287.72 46. 18 49.447 1.5206 1369300 6051 0.6067 33031287- 3 4.0613 289.13 47.67 23.246 1.0615 950900 6072 0.6080 33031287- 4 4 .0456 288.89 47.53 23.257 1.0600 950400 6072 0.6079 33031287- 5 4.1565 288.24 48.96 6. 131 0.5520 495000 6077 0.6079 33031287- 6 4 . 1684 288.29 49.09 6.434 0.5661 507500 6074 0.6076 33032687- 1 4 . 1599 288.36 48.98 6.910 0.5854 524800 6067 0.6069 33032687- 2 4.1513 288.21 48.91 6.710 0.5761 516600 6063 0.6065 33032687- 3 3.9146 287.96 46. 15 48.328 1.4991 1349100 6037 0.6052 33032687- 4 3.9149 288.69 46.03 48.140 1.4925 1340900 6030 0.6046 33032687- 5 4 . 0616 288.94 47.71 21.532 1. 0212 915300 6068 0.6075 33032687- 6 4 .0403 289.43 47.37 21.501 1.0150 908900 6057 0.6064 33110487- 1 4.0023 288.62 47.07 7.997 0.6164 553300 6057 0.6059 33110487- 2 4 .0034 288.56 47 .09 8.320 0.6311 566500 6077 0.6080 33110487- 3 3.8048 287.04 45.01 45.647 1.4388 1299400 6038 0.6053 33110487- 4 3.7956 288.50 44 .65 48.477 1.4733 1326000 6022 0.6038 33110487- 5 3.8356 288.89 45.06 30.776 1.1805 1061000 6035 0.6045 33110487- 6 3.8380 288.97 45.07 30.866 1.1807 1060900 6025 0.6035 33110487- 7 3.9372 289.32 46.18 19.067 0.9441 846600 6060 0.6066 33110487- 8 3.9495 289.43 46.30 19.265 0.9497 851300 6057 0.6063

30

BVaVaVal
Table *. Measured and Calculated Quantities Using Hater in the 3-Inch Orifice Meter,

0.57 Beta Ratio, . 89 §im Roughness

Pipe Diameter = 7.81J> cm Orifice Diameter = 4 .4432 cm

Run ID Temperature Dif Press Flow Rate Pipe C (K) (kPa) (kg/s) Reynolds No. 06/25/87- 1 300.61 2.574 2.282 43972 0.61355 06/25/87- 2 300.64 2.569 2.281 43966 .61371 06/25/87- 3 300 . 69 2.563 2.278 43961 0.61373 06/25/87- 4 300 .75 6.904 3.724 71974 0.61140 06/25/87- 5 300. 78 7.143 3. 790 73292 0.61165 06/25/87- 6 300. 78 6.991 3.755 72605 .61251 06/25/87- 7 300.81 6. 955 3 . 744 72431 0. 61220 06/25/87- 8 300. 83 6.941 3 . 740 72396 0.61226 06/25/87- 9 300. 84 6.910 3 .733 72265 0.61240 06/25/87-10 300. 89 7. 122 3. 784 73352 0.61167 06/25/87-11 300 . 95 7 . 120 3. 784 73458 0.61172 06/25/87-12 300. 99 7.086 3. 775 73340 .61167 06/25/87-13 301. 09 20. 788 6.446 125501 0.60982 06/25/87-14 301.11 20.847 6.456 125739 0. 60985 06/25/87-15 301. 15 20.722 6. 437 125495 0.60998 06/25/87-16 301.23 69. 119 11.725 228953 . 60830 06/25/87-17 301.25 69. 101 11.721 228970 0.60817 06/25/87-18 301.27 68.922 11.705 228766 0. 60816 06/25/87-19 301.32 192.516 19.534 382177 0. 60727 06/25/87-20 301.33 192. 495 19.531 382195 0. 60720 06/25/87-21 301.35 192. 419 19.526 382342 0. 60717 06/26/87-22 300.76 2.582 2.283 44129 .61280 06/26/87-23 300 . 78 2. 567 2.277 44028 0. 61296 06/26/87-24 300.80 2.586 2.286 44228 0.61323 06/26/87-25 300.85 2.528 2.262 43804 0.61359 06/26/87-26 300. 87 2.531 2.262 43827 0.61332 06/26/87-27 300. 89 2.541 2.267 43947 0.61350 06/26/87-28 301.04 6. 981 3.752 72967 0.61245 06/26/87-29 301.05 6.924 3 . 734 72628 .61201 06/26/87-30 301.07 6.872 3.719 72379 .61195 06/26/87-31 301.14 6. 883 3.719 72489 0.61146 06/26/87-32 301.19 6. 863 3.714 72475 0. 61159 06/26/87-33 301.23 6.865 3.715 72547 0.61163 06/26/87-34 301.31 20.636 6. 423 125636 0. 60988 06/26/87-35 301. 34 20.672 6.428 125819 0. 60984 06/26/87-36 301.37 20.612 6.417 125709 0.60968 06/26/87-37 301. 46 68.955 11. 708 229798 0.60819 06/26/87-38 301.52 69.571 11.762 231139 0.60825 06/26/87-39 301.52 68.801 11.695 229823 0.60816 06/26/87-40 301. 60 192.625 19.538 384610 0.60724 06/26/87-41 301. 60 192.835 19.543 384708 0.60706 06/26/87-42 301.61 192.796 19.547 384865 0.60724

31
Table 5. Measured and Calculated Quantities Using Eifcrogen Gas In the 3-Inch Orifice Meter,

0.57 Beta Satio, 0.89 la Roughness

Pipe Diame

Pressure

ier = 7 .816

Temperature

cm

Density

(kg/m3

)

Orifice Diameter 4.4432 cm

Run ID Dif Press Flow Rate Pipe c CY 2 (MPa) (K) (kPa) (kg/s) Reynolds No 34042987- 1 3 . 7854 287.31 44 .74 49.069 2.0839 1880300 6056 0.6071 34042987- 2 3.7867 288.01 44 .63 49.117 2.0633 1876600 6058 0.6073 34042987- 3 4 . 1497 286.64 49.18 3.498 0.5865 527700 6106 0.6107 34042987- 4 4 . 1264 286.46 48.94 4.374 0.6552 590000 6115 0.6116 34042987- 5 4 .0878 286.18 48.54 11.155 1.0401 937600 6099 0.6102 34042987- 6 4 .0922 285.92 46.64 11.133 1.0401 938200 6099 0.6102 34042987- 7 3.9276 284.69 46.89 27.417 1.6005 1450900 6085 0.6094 34042987- 8 3.9266 284 .61 46.90 27.200 1.5925 1443900 6078 0.6087 34042987- 9 3. 9320 288.79 46.21 27.468 1.5876 1424800 6074 0.6082 34102687- 1 4 .0005 288.26 47. 12 11.319 1.0261 921200 6062 0.6065 34402687- 2 3.9669 286. 89 46.96 11.212 1.0190 918200 6059 0.6062 34102687- 3 3.7048 288. 82 43.53 50.671 2.0776 1869200 6022 0.6039 34102687- 4 3.7143 290.95 43.29 50.994 2.0807 1862200 6028 0.6044 34102687- 5 3.8582 289.23 45.26 29.403 1.6157 1449700 6036 0.6045 34102687- 6 3.8440 289.53 45.05 29.541 1.6157 1448800 6036 0.6045 34102687- 7 4 .0786 290.04 47.71 3.629 0.5866 523900 6086 0.6087 34102687- 8 4 .0744 288. 59 47.93 3 .987 0.6151 551300 6074 0.6075 34102787- 1 3.9895 285.87 47 .42 12.180 1.0665 963100 6054 0.6058 34102787- 2 3. 9876 288. 13 46.99 12.254 1.0666 958000 6064 0.6068 34102787- 3 3.7754 287 . 87 44.52 47.311 2.0283 1827600 6018 0.6033 34102787- 4 3. 7794 288. 50 44 .46 47 . 400 2.0302 1826400 6022 0.6036 34102787- 5 3. 8867 287 .39 45.92 28.758 1.6078 1448500 6031 0.6040 34102787- 6 3. 8862 284 .77 46. 38 28.651 1.6129 1462300 6031 0.6040 34102787- 7 4. 1293 284.52 49.35 3 . 497 0.5854 529500 6084 0.6085 34102787- 8 4 . 1274 287 .04 48.84 3.904 0.6149 552800 6080 0.6081 34111287- 1 3.8924 288.27 45.84 12. 166 1.0469 941100 6048 0.6051 34111287- 2 3.8876 288.23 45.78 12.136 1.0449 939400 6047 0.6051 34111287- 3 3.8141 287 .79 44 .99 26.930 1.5394 1386600 6028 0.6037 34111287- 4 3. 8136 287 .64 45.01 29.256 1.6040 1445400 6024 0.6033 34111287- 5 4 .0385 288.33 47.55 4 .438 0.6465 580000 6075 0.6076 34111287- 6 4 .0249 288.45 47.37 4.568 0.6536 586300 6065 0.6067 34111287- 7 3.7281 286.28 44.23 47.514 2.0249 1832600 6015 0.6030 34111267- 8 3.6852 287.51 43.51 47.085 1.9964 1802300 6005 0.6020

Table 6. Measured and Calculated Quantities Using Hater in the 3-Inch Orifice Meter,

0.57 Beta Ratio, 4 . 1 ftm Roughness

Pipe Diameter = 7.813 cm Orifice Diameter 4 4432 cm

Run ID Temperature Dif Press Flow Rate Pipe C (K) (kPa) (kg/s) Reynolds No. 06/30/87- 2 301.60 2.572 2.277 44896 0.61257 06/30/87- 3 301. 62 2.573 2.279 44941 0.61280 06/30/87- 4 301.68 2.553 2.272 44850 0.61316 06/30/87- 5 301.74 7.045 3.767 74483 0.61220 06/30/87- 6 301. 76 7.048 3.766 74480 0.61182 06/30/87- 7 301. 77 7. 036 3.762 74417 0.61167 06/30/87- 8 301. 82 7 . 044 3.759 74456 0.61085 06/30/87- 9 301. 87 7.055 3.762 74604 0.61098 06/30/87-10 301. 92 7.034 3 .756 74566 0.61092 06/30/87-11 302.05 20.900 6.459 128561 0.60940 06/30/87-12 302.08 20.917 6.462 128712 0.60949 06/30/87-13 302. 12 20.870 6.454 128658 0.60941 06/30/87-14 302.15 68. 958 11.701 233386 0.60778 06/30/87-15 302.19 68.978 11.702 233607 0.60776 06/30/87-16 302.20 68.950 11.705 233711 0.60803 06/30/87-17 302.24 192. 783 19.543 390625 0.60713 06/30/87-18 302.24 193.945 19.591 391587 0.60680 06/30/87-19 302.24 192.072 19.505 389869 0.60708 06/30/87-20 302.27 192.787 19.538 390780 0.60699 06/30/87-21 302.26 192.790 19.536 390665 .60693 06/30/87-22 302.27 192.735 19.530 390613 0.60681 07/01/87-23 301. 58 2.574 2.277 44877 0.61238 07/01/87-24 301.60 2.577 2.280 44940 0.61256 07/01/87-25 301.63 2.566 2.274 44851 0.61227 07/01/87-26 301. 70 7.154 3.797 75001 0.61228 07/01/87-27 301. 71 7.067 3.769 74476 0.61160 07/01/87-28 301.73 7.092 3.776 74636 0.61155 07/01/87-29 301.82 7 .059 3. 763 74536 0.61089 07/01/87-30 301.87 7.050 3.760 74568 0.61088 07/01/87-31 301. 92 7.041 3.759 74618 0.61106 07/01/87-32 302.04 21.123 6.493 129205 0.60935 07/01/87-33 302.07 21. 185 6.504 129507 0.60950 07/01/87-34 302. 12 21. 190 6. 503 129631 0.60937 07/01/87-35 302.21 68.817 11.692 233510 0.60796 07/01/87-36 302.22 68.974 11.707 233900 0.60803 07/01/87-37 302.25 68.806 11.690 233713 0.60790 07/01/87-38 302.29 192.728 19.530 390772 0.60661 07/01/87-39 302. 31 193.329 19.566 391663 0.60700 07/01/87-40 302.30 193.062 19.556 391367 0.60712

32
Table 7. Measured and Calculated Quantities Using litrogen Gas in the 3-Inch Orifice Meter,

0.57 Beta Ratio, 4.1 iim Roughness

Run ID

34031787- 1 34031787- 2 34031787- 3 34031787- 4 34031787- 5 34031787- 6 34102987- 1 34102987- 2 34102987- 3 34102987- 4 34102987- 5 34102987- 6 34102987- 7 34102987- 8 34103087- 1 34103087- 2 34103087- 3 34103087- 4 34103087- 5 34103087- 6 34103087- 7 34103087- 8

Table 1 B.

Pipe Diameter TM 7.813 cm Orifice Diameter = 4.4432 cm

'ressure Temperature Density Dif Press Flow Rate Pipe c CY 2 (MPa) (K) Ckg/m 3

) (kPa) (kg/s) Reynolds No

4 . 1429 289.01 48.66 4 .281 0.6456 577700 .6106 0.6107

4 . 1604 288.92 48.88 3. 773 0.6067 542900 .6098 0.6099

3. 9486 289.21 46. 33 25.931 1.5427 1383000 .6066 0.6074

3 .9492 289. 14 46.35 25.849 1. 5421 1382700 .6073 0.6081 3.8051 287.57 44 .93 48.621 2.0906 1884900 .6078 0.6093

3. 8060 288.28 44 .81 48.562 2.0770 1869400 .6062 0.6077 3.9357 287 .27 46.53 11.730 1.0397 936700 .6072 0.6075

3. 9266 287.21 46.43 11.600 1.0321 930100 .6067 0.6071

4 .0635 286.86 48. 12 4 . Ill 0.6268 564400 .6083 0.6084

4 .0767 286.69 48.31 4.521 0.6604 594800 .6099 0.6101 3.7448 288.00 44 . 14 48.607 2.0543 1851700 .6038 0.6054

3. 7414 287 .97 44. 10 48. 127 2.0402 1839200 .6029 . 6044 3.8575 286.49 45.73 28.816 1.6081 1452800 .6037 0.6046 3.8551 286.37 45.73 28. 916 1.6111 1456000 .6039 0.6048 3.9515 288.31 46.53 12.628 1.0748 965700 .6048 0.6052 3.9559 288.30 46.58 12.566 1.0722 963300 .6045 0.6049

4. 1104 288.51 48.37 3.949 0.6155 551700 .6080 0.6081

4 . 0996 288. 53 48.24 4 .640 . 6661 597100 6077 0.6078 3.7661 286.88 44 . 58 46.628 2.0176 1823100 .6026 0.6040

3 .7636 286.61 44 . 60 45.970 2.0028 1811000 .6023 0.6038

3 .8663 286. 96 45. 76 29. 169 1.6180 1460000 .6036 .6045

3 .8561 286.86 45.65 29. 166 1.6122 1455300 .6022 0.6031

Measured and Calculated Quantities Dsing Hater in the 3-Inch Orifice Meter,

0.57 Beta Ratio, 7.6 iim Roughness

Pipe Diameter - 7.811 cm Orifice Diameter = 4 .4432 cm

Run ID Temperature Dif Press Flow Rate Pipe C

(K) (kPa) Ckg/s) Reynolds No. 07/13/87- 1 301. 48 2.530 2.263 44519 0.61359 07/13/87- 2 301.51 2.523 2.261 44498 0.61376 07/13/87- 3 301.54 2.498 2.250 44313 0.61393 07/13/87- 4 301. 62 7. 075 3. 779 74570 0.61283 07/13/87- 5 301. 63 7.076 3.775 74495 0.61205

07/13/87- 6 301.64 7.093 3.780 74603 0.61213

07/13/87- 7 301.77 7.063 3.767 74566 0.61128

07/13/87- 8 301.80 7 . 070 3.770 74677 0.61152

07/13/87- 9 301. 84 7 .034 3.759 74535 0.61139 07/13/87-10 301.88 21.023 6. 481 128594 0.60963 07/13/87-11 301. 90 21.004 6. 478 128592 0.60964 07/13/87-12 301.93 20 .931 6. 466 128438 0.60957 07/13/87-13 301.98 69.050 11.721 233061 0.60837 07/13/87-14 302.00 69.065 11. 719 233122 0.60821 07/13/87-15 302.01 68.992 11.715 233088 0.60831 07/13/87-16 302.10 192.657 19.553 389769 0.60758 07/13/87-17 302. 12 192.770 19.556 389989 0.60749 07/13/87-18 302. 13 192.599 19.551 389979 0.60762 07/15/87-19 303. 71 2.535 2.265 46722 0.61361 07/15/87-20 303. 73 2.544 2.268 46824 0.61352 07/15/87-21 303.74 2.511 2.255 46557 0.61399 07/15/87-22 303.83 7 .059 3.780 78195 0.61383 07/15/87-23 303 .83 7.137 3.789 78377 0.61190 07/15/87-24 303.84 7 .052 3.767 77937 0.61200 07/15/87-25 303.91 7.034 3.758 77860 0.61129 07/15/87-26 303.93 7.017 3.754 77817 0.61143 07/15/87-27 303.96 7.028 3.757 77918 0.61139 07/15/87-28 304 02 21.069 6.484 134641 0.60942 07/15/87-29 304 .04 21.081 6.486 134731 0.60939 07/15/87-30 304 .05 20.882 6.456 134149 0.60952 07/15/87-31 304 . 10 69.077 11.715 243669 0.60810 07/15/87-32 304 . 12 68.929 11.703 243519 0.60813 07/15/87-33 304. 12 68.833 11.698 243408 0.60828 07/15/87-34 304 . 16 192.596 19.543 406983 0.60752 07/15/87-35 304 . 16 192.849 19. 553 407207 0.60746 07/15/87-36 304 . 17 192.732 19.550 407224 0.60754

33
Table 9. Measured and Calculated Quantities Using Ritrogen Gas in the 3-Inch Orifice Meter,

0.57 Beta Ratio, 7.6 pat Roughness

Run ID

34031387- 1 34031387- 2 34031387- 3 34031387- 4 34031387- 5 34031387- 6 34110387- 1 34110387- 2 34110387- 3 34110387- 4 34110387- 5 34110387- 6 34110387- 7 34110387- 8 34110487- 1 34110487- 2 34110487- 3 34110487- 4 34110487- 5 34110487- 6 34110487- 7 34110487- 8 34110487- 9

Pipe Diameter = 7.811 cm Orifice Diameter = 4 . 4432 cm

Pressure Temperature Density Dlf Press Flow Rate Pipe c CY 2 (MPa) (K) (kg/m 3

) (kPa) (kg/s) Reynolds No 3.9152 287.43 46.25 25.581 1.5317 1380200 6069 0.6077 3.9159 288.27 46. 11 25.465 1.5243 1370800 6063 0.6071

4.1161 289.67 48.22 4.066 0.6233 557300 6075 0.6077

4 . 1236 289. 73 48. 30 3.610 0. 6036 539600 6074 0.6075

3. 7970 286.47 45.02 48.299 2.0759 1877700 6061 0.6076

3. 7983 287.86 44 . 79 48. 189 2.0685 1864600 6061 0.6076 3.7591 289. 56 44 .04 49.297 2.0651 1854700 6033 0.6048

3.7631 289.20 44. 15 49. 162 2.0653 1856400 6034 0.6050

3.8977 287 . 11 46. 10 30.523 1.6647 1501400 6047 0.6057 3.8769 288.09 45.68 30.697 1.6620 1495800 6048 . 6057

3 . 9699 288. 73 46.67 12. 580 1.0761 966000 6058 0.6061

3 .9737 288. 78 46.71 12. 631 1. 0800 969300 6065 . 6068 4.1152 289.67 48.21 4 .094 0.6265 560100 6086 . 5087

4 . 1150 289.67 48.21 4.443 . 6520 582900 6079 0.6081

3.6980 287.94 43.59 47 . 444 2.0242 1826400 6059 .6075 3.6952 287.99 43.55 47.255 2.0184 1821100 6057 . 6072

3 .8870 288.84 45.67 12.850 1.0791 969300 6075 . 6079 3.8868 289.05 45.63 13.062 1.0865 975600 6070 0.6074 4.0239 289.91 47.09 4.231 0.6293 562900 6084 0. 6085

4 .0343 289.57 47.28 4 .062 0. 6185 553600 6091 0.6092 3.8236 287.77 45. 11 26.854 1.5491 1396200 6066 0.6075

3.8303 287.78 45. 19 26.693 1. 5461 1393300 6067 0.6076

3.6888 287.28 43.59 49.405 2.0678 1868900 6065 0.6081

Table 10. Measured and Calculated Quantities Using Hater in the 3-Inch Orifice Meter, 0.65 Beta Ratio, 0.89 fim Roughness

Pipe Diameter = 7.816 cm Orifice Diameter 5 0780 cm

Run ID Temperature Dif Press Flow Rate Pipe C (K) (kPa) (kg/s) Reynolds No. 06/24/87- 1 299. 58 2.579 3. 133 58997 0. 61699 06/24/87- 2 299.64 2.620 3 . 158 59542 0. 61709 06/24/87- 3 299. 70 2.534 3 . 108 58687 0.61759 06/24/87- 4 299. 78 7.323 5.257 99454 0.61449 06/24/87- 5 299.84 7.034 5. 156 97651 0.61482 06/24/87- 6 299.87 7.006 5. 145 97523 0.61487 06/24/87- 7 299.94 20.928 8. 858 168145 0.61245 06/24/87- 8 299.97 21.258 8.927 169560 . 61240 06/24/87- 9 299.99 21.282 8.930 169699 0.61229 06/24/87-10 300.07 69. 105 16.036 305257 . 61017 06/24/87-11 300. 08 69. 037 16.038 305369 0.61055 06/24/87-12 300.09 69. 038 16. 037 305421 .61053 06/24/87-13 300. 13 69. 139 16. 053 306045 .61067 06/24/87-14 300. 15 68.565 15. 985 304884 . 61063 06/24/87-15 300. 16 69.306 16.072 306597 0. 61064 06/24/87-16 300.23 192.670 26. 740 510891 . 60936 06/24/87-17 300.24 192. 548 26. 738 510956 0.60950 06/24/87-18 300 .26 192.555 26.743 511277 . 60961 06/25/87-19 299. 87 2.563 3. 122 59175 0.61688 06/25/87-20 299.92 2.569 3. 127 59328 0.61699 06/25/87-21 299.97 2.561 3. 123 59321 0.61723 06/25/87-22 300 . 12 6. 948 5. 121 97616 0.61455 06/25/87-23 300. 16 6. 966 5. 130 97857 0.61476 06/25/87-24 300 .20 6.940 5. 119 97744 0.61469 06/25/87-25 300.29 21.162 8.904 170328 0.61222 06/25/87-26 300.33 21. 172 8.905 170496 0.61215 06/25/87-27 300. 36 21.178 8. 909 170694 .61238 06/25/87-28 300. 43 68.890 16.021 307413 0.61058 06/25/87-29 300.44 68.686 15.993 306950 0. 61043 06/25/87-30 300.45 69.129 16.049 308080 0.61058 06/25/87-31 300. 50 69. 160 16.053 308496 0.61062 06/25/87-32 300. 52 68.982 16.034 308264 0.61069 06/25/87-33 300.53 69. 014 16.028 308272 .61029 06/25/87-34 300. 62 192.258 26.720 514905 0.60958 06/25/87-35 300.61 192.308 26.724 514868 0.60958 06/25/87-36 300.61 192.646 26. 746 515299 0.60956

34

>>>>
Table 11. Measured and Calculated Quantities Using litrogen Gas in the 3-Inch Orifice

Meter. 0.65 Beta Ratio. 0.89 va Roughness

Run ID

35102687- 1 35102687- 2 35102687- 3 35102687- 4 35102687- 5 35102687- 6 35102687- 7 35102687- 8 35102887- 1 35102887- 2 35102887- 3 35102887- 4 35102887- 5 35102887- 6 35102887- 7 35102887- 8

Table 12.

Pipe Diame ter = 7.816 cm Orifice Diameter = 5.0780 cm

'ressure Temperature Density

(kg/m 3

) Dif Press Flow Rate Pipe c CY 2 (MPa) (K) (kPa) (kg/s) Reynolds N o . 3. 9139 288.99 45.96 9.288 1.2576 1128200 .6091 0.6093

3 .9095 288.67 45.97 9.266 1.2541 1126100 6031 0.6084

4 .0613 287.36 48.00 2.879 0. 7182 645700 .6116 0.6117

A. 0585 287.86 47 .87 3.056 0.7389 663600 6116 .6117

3 .6432 278.97 44 .47 31. 679 2.2656 2090100 6035 .6045

3 .6498 276. 91 44 . 92 31.379 2.2644 2099700 6031 . 6040 3.8027 285.32 45.29 19. 732 1.8072 1638000 6047 . 6053

3 . 8036 289. 76 44.53 20.202 1.8132 1625800 6046 . 6052

4 . 0884 286. 48 48. 48 2. 840 0.7171 645900 .6118 . 6119

4. 1002 286. 49 48. 62 2. 529 0.6756 608400 6100 .6100

3 .8875 289. 14 45. 63 18. 309 1.7525 1572000 6065 0.6070 3.8675 287.35 45.70 18. 400 1.7528 1579600 6046 0.6051

3. 6830 282.47 44 .34 30.973 2.2331 2041200 6025 0.6034

3 . 6789 281.44 44 . 47 30. 589 2.2251 2039100 6032 0.6041 3.9204 288.88 46.06 9.902 1.2971 1163900 6078 0.6081 3.9257 291.05 45. 74 10.274 1. 3170 1175600 6079 0.6082

Measured and Calculated Quantities Using Water in the 3-Inch Orifice Meter, 0.65 Beta Ratio, 4.1 itm Roughness

Pipe Diameter - 7.813 cm Orifice Diameter = 5 0780 cm

Run ID Temperature Dif Press Flow Rate Pipe C (K) (kPa) (kg/s) Reynolds No. 06/29/87- 1 300 .68 2.558 3. 119 60276 0. 61698 06/29/87- 2 300.75 2.621 3 . 158 61104 0.61686 06/29/87- 3 300. 79 2.624 3 . 159 61179 0.61683 06/29/87- 4 300.91 7 . 088 5.171 100411 0. 61437 06/29/87- 5 300. 94 7.081 5. 170 100463 0.61445 06/29/87- 6 300.98 7 . 088 5. 172 100590 0.61443 06/29/87- 7 301.07 20 .707 8.806 171610 0.61211 06/29/87- 8 301.09 20.695 8. 804 171653 0.61218 06/29/87- 9 301.11 20.711 8.808 171794 0.61219 06/29/87-10 301. 17 69.177 16. 050 313429 0.61036 06/29/87-11 301.19 68.940 16. 027 313112 0.61053 06/29/87-12 301.20 69.089 16.039 313427 0.61035 06/29/87-13 301.28 68.941 16.026 313698 0.61050 06/29/87-14 301.27 69. 192 16.056 314213 0.61053 06/29/87-15 301.28 69.286 16.066 314486 0.61051 06/29/87-16 301.37 192. 642 26.744 524627 0.60950 06/29/87-17 301. 38 192.955 26.757 524981 0.60929 06/29/87-18 301.39 193. 394 26. 794 525810 0.60943 06/30/87-19 300.90 2.616 3. 152 61183 0.61630 06/30/87-20 300. 95 2.618 3. 153 61286 0. 61634 06/30/87-21 301. 00 2. 610 3. 150 61292 0. 61670 06/30/87-22 301. 08 7 .034 5. 154 100459 0.61466 06/30/87-23 301. 12 7 .021 5. 148 100432 0.61456 06/30/87-24 301. 16 7 .019 5. 150 100544 0.61483 06/30/87-25 301.24 20. 846 8.838 172849 0.61227 06/30/87-26 301.27 20.851 8.837 172950 .61217 06/30/87-27 301.29 20.826 8.831 172900 0.61209 06/30/87-28 301. 39 69.019 16.034 314666 0.61050 06/30/87-29 301.40 69. 106 16.043 314910 0.61045 06/30/87-30 301. 42 69. 167 16.047 315125 0.61034 06/30/87-31 301.49 69.217 16.059 315818 0.61056 06/30/87-32 301.50 69.260 16.063 315968 0.61053 06/30/87-33 301.50 69.280 16.067 316037 0.61058 06/30/87-34 301.54 193. 164 26.774 527105 0.60937 06/30/87-35 301.52 193.039 26.772 526836 0.60951 06/30/87-36 301. 50 193.459 26.800 527166 0.60948

35
Table 13. Measured and Calculated Quantities Using Ritrogen Gas in the 3-Inch Orifice

Meter, 0.65 Beta Ratio. 4.1 iim Roughness

Pice Diameter - 7.813 cm Orifice Diameter = 5.0780 cm

Run ID Pressure Temperature Density

(kg/m 3

) Dif Press Flow Rate Pipe c CY 2 (MPa) (K) (kPa) (kg/s) Reynolds No 35102887- 1 3.8647 286.71 45.78 17. 504 1.7150 1548500 6060 0.6065 35102887- 2 3.8717 286.62 45.88 17.380 1. 7089 1543100 6053 0.6058 35102887- 3 3.9568 290. 52 46.20 8. 599 1.2133 1084300 6091 0.6093 35102887- 4 3.9384 290.73 45.95 8. 649 1.2117 1082600 6082 0.6084 35102887- 5 4.0855 291.40 47.55 2.639 0.6834 608500 6106 0.6107 35102887- 6 4.0955 290.63 47. 80 2.958 0.7268 648300 6117 0.6118 35102887- 7 3. 7050 283.79 44.38 30.070 2.2161 2019100 6064 . 6073 35102887- 8 3.6974 283. 14 44.40 29.798 2.1976 2005700 6040 0.6049 35102987- 1 3.6909 287.95 43.51 31.066 2.2353 2016300 6077 0.6086 35102987- 2 3. 7134 286.81 43.96 29.671 2.1939 1983900 6072 . 6080 35102987- 3 3.9489 288. 13 46.53 10.300 1.3364 1201300 6108 . 6111 35102987- 4 3. 9341 288.20 46.34 10.380 1.3369 1201700 6099 . 6102 35102987- 5 3.8459 287. 46 45. 43 18. 746 1.7744 1599500 6081 .6086 35102987- 6 3.8488 287.64 45.43 18.652 1.7658 1591000 6067 6072 35102987- 7 4.0805 288.38 48.04 2.677 0.6912 620000 6102 0.6103 35102987- 8 4 . 0840 288.73 48.02 2.747 0.7003 627600 6104 0.6104 35103087- 1 3.7126 288.02 43.75 29.402 2. 1652 1952200 6034 .6043 35103087- 2 3.7174 287.96 43.82 29.477 2. 1709 1957600 6038 0.6046 35103087- 3 3 .9386 287 . 91 46. 45 9. 497 1.2741 1146100 6070 0.6073 35103087- 4 3.9271 288.04 46.29 9. 599 1.2797 1150900 6075 0. 6077 35103087- 5 3 .8529 287.63 45.48 18.317 1. 7431 1570500 6040 0.6045 35103087- 6 3.8462 287.65 45. 40 18. 129 1.7336 1562100 6044 0.6049 35103087- 8 4 . 0740 289.02 47.85 2.870 0.7141 639600 6100 0.6101

Table 1* . Measured and Calculated Quantities Osing Hater in the 3-Inch Orifice Meter, 0.65 Beta Ratio, 7.6 iim Roughness

Pipe Diameter = 7.811 cm Orifice Diameter = 5 0780 cm

Run ID Temperature Dif Press Flow Rate Pipe C (K) (kPa) (kg/s) Reynolds No. 07/13/87- 1 302. 15 2.494 3 . 081 61475 . 61702 07/13/87- 2 302. 18 2.497 3. 085 61604 0.61749 07/13/87- 3 302.21 2. 484 3.077 61486 0.61750 07/13/87- 4 302.26 7.004 5. 143 102881 0.61463 07/13/87- 5 302.29 7.019 5. 147 103042 0.61454 07/13/87- 6 302.33 7.015 5. 147 103118 0.61467 07/13/87- 7 302.36 20.959 8.864 177693 0. 61238 07/13/87- 8 302.39 20. 949 8.861 177761 0. 61237 07/13/87- 9 302.40 20. 888 8. 850 177570 0.61248 07/13/87-10 302.46 69. 180 16.066 322757 0.61097 07/13/87-11 302. 47 68.965 16. 044 322383 0.61108 07/13/87-12 302. 48 68.978 16.047 322514 0.61115 07/13/87-13 302.53 69. 148 16.069 323305 0.61125 07/13/87-14 302. 55 69.367 16.097 323994 0.61133 07/13/87-15 302.55 69.471 16. 107 324203 0. 61127 07/13/87-16 302.61 193.393 26.848 541073 0.61068 07/13/87-17 302.61 193.337 26.847 541045 0.61073 07/13/87-18 302.63 193.280 26.843 541193 0.61074 07/14/87-19 302. 10 2.543 3. 103 61851 0.61535 07/14/87-20 302. 15 2.526 3.093 61723 0.61559 07/14/87-21 302.20 2.507 3.083 61584 0.61585 07/14/87-22 302.27 2.486 3. 070 61436 . 61589 07/14/87-23 302.31 2. 488 3.071 61499 0. 61584 07/14/87-24 302.35 2.482 3.068 61502 0.61601 07/14/87-25 302.46 6.973 5. 128 103025 0.61428 07/14/87-26 302.48 6.993 5. 136 103227 .61432 07/14/87-27 302. 51 6.981 5.132 103210 0. 61440 07/14/87-28 302.78 20.838 8.838 178781 0.61241 07/14/87-29 302.81 20.833 8.835 178830 0.61227 07/14/87-30 302.82 20.790 8.828 178734 0.61245 07/14/87-31 302. 89 69.099 16. 057 325573 0.61104 07/14/87-32 302. 88 68.864 16. 034 325032 0.61119 07/14/87-33 302.89 68.996 16.045 325328 0.61104 07/14/87-34 303.05 68.849 16.036 326231 0.61136 07/14/87-35 303.05 69.053 16.061 326722 0.61137 07/14/87-36 303.06 68.876 16.042 326410 0.61145 07/14/87-37 303.13 191.549 26.723 54 4 53 8 0.61078 07/14/87-38 303 . 14 192.371 26.781 545844 .61081 07/14/87-39 303. 15 192.531 26.798 546298 0.61094

36
Table 15. Measured and Calculated Quantities Using Hitrogen Gas in the 3-Inch Orifice

Meter. 0.65 Beta Ratio. 7.6 tarn Roughness

Run ID

35031387- 1 35031387- 2 35031387- 3 35031387- 4 35031387- 5 35031387- 6 35031387- 7 35110387- 1 35110387- 2 35110387- 3 35110387- 4 35110387- 5 35110387- 6 35110387- 7 35110387- 8 35110387- 9 35110387-10

35110687- 1 35110687- 2 35110687- 3 35110687- 4 35110687- 5 35110687- 6 35110687- 7 35110687- 8 35110687- 9

Pipe Diame ter =• 7. 811 cm Orifice Diameter = 5.0780 cm

Pressure Temperature Density Dif Press Flow Rate Pipe c CY 2 (MPa) (K) (kg/m3

) (kPa) (kg/s) Reynolds N o . 4 . 1351 288.36 48.68 3.254 0. 7667 687500 .6097 0.6098

4. 1387 288.09 48. 78 3.199 0.7651 686500 .6130 0.6131

4 . 1 4 2

1

288.44 48.75 3.104 0. 7546 676500 .6140 0.6140

3. 7025 285.66 44.03 32.321 2.2883 2076200 .6062 0.6071

3. 7040 286. 03 43.98 32.062 2.2827 2069200 .6075 0.6084 3.8884 289.54 45.57 20 . 129 1.8432 1653100 .6085 0.6091 3.8878 289.24 45.61 20. 183 1.8485 1659000 .6091 0.6097 3.9744 288.58 46. 75 9. 039 1.2554 1127200 .6109 0.6112 3.9625 287.64 46. 78 8.912 1.2442 1119900 .6097 0.6099 3.7055 288.69 43.56 30.695 2.2235 2002400 .6077 0.6086 3.6926 288.06 43. 51 30.414 2.2121 1995500 .6077 0.6086

4. 1068 288. 58 48.31 3 .029 0. 7392 662700 .6116 0.6117 4.0998 288.87 48.17 2.721 0.7019 628900 6136 .6137 3.8575 287.37 45.58 18.417 1.7710 1597100 6112 0.6118

3. 8608 287. 16 45.66 18.294 1. 7643 1591900 6105 0.6110 3.9700 287.66 46. 86 9. 176 1.2694 1142400 6125 0.6127 3.9495 287.81 46. 59 8.937 1.2510 1125700 6134 0.6136

3. 7047 287.74 43. 70 28.680 2. 1579 1947800 6092 0. 6100

3 .6998 287.82 43.63 28.697 2.1537 1943700 6083 0.6091 3.8248 287.61 45. 15 19.229 1.7922 1616000 6082 0.6088 3.8282 287.72 45. 17 19. 176 1. 7897 1613200 6081 0.6086

3 .9166 288.56 46.07 9.348 1.2654 1137100 6100 0.6102

3. 9195 288.61 46.09 9.457 1.2725 1143300 6097 0.6100

4 . 0616 288.68 47.76 2.824 . 7136 639900 6149 0.6150

4 .0738 288. 79 47.88 2.702 .6984 626000 6145 0.6146

3 . 7140 288.31 43.72 29.026 2. 1711 1956800 6091 0.6100

Table 16. Measured and Calculated Quantities Dsing Hater in the 3-Inch Orifice Meter.

0.73 Beta Ratio, 0.89 pat Roughness

Pipe Diameter - 7.816 cm Orifice Diameter « 5 7132 cm

Run ID Temperature Dif Press Flow Rate Pipe C (K) (kPa) (kg/s) Reynolds No. 06/22/87- 1 297.52 2.547 4.230 76022 0.61740 06/22/87- 2 297.57 2.541 4.226 76047 0.61761 06/22/87- 3 297.62 2.542 4.226 76142 0.61742

06/22/87- 4 297 . 76 20.922 12.012 217092 .61170 06/22/87- 5 297.77 21.195 12.085 218458 .61144 06/22/87- 6 297.80 21.004 12.031 217624 0.61145

06/22/87- 7 297.95 7.066 7.012 127292 0. 61447 06/22/87- 8 297.99 7.115 7.037 127855 0.61452 06/22/87- 9 298.02 7.077 7.017 127575 0.61440 06/22/87-10 298. 10 20.961 12.019 218921 0.61153 06/22/87-11 298. 13 21. 140 12.077 220113 .61184 06/22/87-12 298.16 20.800 11.978 218455 0.61178 06/22/87-13 298.27 69.366 21.796 398490 0.60961 06/22/87-14 298.28 70.138 21.900 400575 .60915 06/22/87-15 298. 31 69.124 21.788 398780 0.61045 06/22/87-16 298.46 192.474 36.205 664857 0.60792 06/22/87-17 298.47 192.478 36.213 665147 0.60804 06/22/87-18 298.47 192.747 36.234 665524 0.60796 06/23/87-19 298. 53 2.579 4.256 78278 0.61737 06/23/87-20 298.58 2.596 4.270 78616 0.61729 06/23/87-21 298.63 2.616 4.285 78984 0.61715 06/23/87-22 298.78 6.976 6.968 128886 0.61454 06/23/87-23 298.82 7.013 6.986 129327 0.61452 06/23/87-24 298.84 7.028 6.992 129508 0.61443 06/23/87-25 299.31 20.759 11.964 223923 0.61173 06/23/87-26 299.31 20.769 11.963 223903 0.61152 06/23/87-27 299.34 20.866 11.993 224616 0.61164 06/23/87-28 299.41 21.190 12.088 226792 0.61177 06/23/87-29 299.42 21.276 12.109 227231 0.61159 06/23/87-30 299.43 21.171 12.078 226711 0.61156 06/23/87-31 299.87 69.293 21.771 412641 0.60933 06/23/87-32 299.90 69.299 21.778 413054 0.60952 06/23/87-33 299.93 69.397 21.783 413421 0.60924 06/23/87-34 300.03 192.080 36. 159 687721 0.60786 06/23/87-35 300.03 194.617 36.398 692272 0.60788 06/23/87-36 300.03 192.240 36.182 688167 0.60800

37
Table 17. Measured and Calculated Quantities Using Nitrogen Gas in the 3-Inch Orifice

Meter, 0.73 Beta Ratio, 0.89 /in Roughness

Run ID

36042 36042

36042

36042

36042

36042

36042

36042 36042

36042

36042

36042 36042

36042

36042

36042

36042

36042 36111

36111 36111

36111

36111

36111

36111 36111

36111

36111 36111

36111

36111 36111 36111

36111

787-

787- 787- 787-

787-

787-

787- 787-

787- 987-

987-

987-

987- 987-

987-

987-

987- 987-

087- 087-

087-

087- 087-

087-

087- 087-

287- 287-

287- 287-

287-

287-

287-

287-

Pipe Di ameter " 7.816 cm Orifice Diameter = 5.7132 cm

Pressure Temperature Density

(kg/m3

) Dif Press Flow Rate Pipe c cv 2 (MPa) (K) (kPa) (kg/s) Reynolds No 3.8189 287.15 45.16 11.538 1.8650 1682800 6021 0.6024 3.8276 288.01 45.11 11.573 1.8701 1683600 6031 0.6034 4.0476 288.81 47.57 2.935 0.9727 871800 6070 0.6070 4.0666 289. 12 47.74 2.942 0.9768 874500 6076 0.6077 3.7299 288.36 43.90 17.487 2.2617 2036900 6014 0.6019 3.7025 288.26 43 .59 18. 183 2.2981 2070800 6014 0.6018 3.9325 287.86 46.38 6.673 1.4478 1302300 6066 0.6068 3.9630 287.52 46.81 6.712 1.4603 1314100 6073 0.6075 3.9290 288.37 46.25 6.695 1.4454 1298600 6054 0.6056

3. 7103 284 . 93 44 .24 18.089 2.3112 2099400 6019 0.6024 3.6997 285.42 44 .04 18.013 2.3028 2089500 6024 0.6029 3.9315 286.82 46.55 6.974 1.4798 1334400 6054 0.6055

3. 9430 287.01 46.66 6.457 1.4315 1290100 6079 0.6081

3.9664 287.83 46.79 6.505 1.4331 1288700 6056 0.6057

4 .0760 288.75 47.92 2.769 0.9511 852300 6088 0.6089 4.0765 288.68 47.94 2.755 0.9512 852500 6103 0.6104 3.8729 288.69 45.53 12. 147 1.9324 1735900 6055 0.6058

3. 8779 288.21 45.67 12. 104 1.9319 1737400 6055 0.6058 3.8886 288.29 45. 79 6. 404 1.4040 1262000 6044 0.6046

3 . 8738 288.27 45.61 6.351 1.3960 1255200 6047 0.6048 3.6582 288.22 43.08 17.021 2.2169 1998600 6033 0.6037 3.6580 287.55 43. 16 16.899 2.2076 1993400 6022 0.6026 4.0095 289.72 46.96 2. 955 0. 9703 868000 6074 0.6075

4 .0047 289.98 46.86 3.036 0.9826 878400 6074 0.6075 3.7803 288.81 44.42 12.087 1.8973 1705500 6035 0.603B 3.8027 289.13 44 .63 12.013 1.8956 1702200 6034 0.6037

3.8704 288.76 45.49 5.772 1.3303 1194700 6053 0.6054 3.8916 288.73 45.75 5.824 1.3419 1204900 6061 0.6062 3.9675 289.28 46. 54 2.650 0.9151 819900 6076 0.6076 3.9720 289.27 46.60 2.676 0.9214 825500 6084 0.6085

3. 7580 288.03 44 .29 11.885 1.8787 1692400 6035 0.6038 3.7692 288.28 44 .38 11.771 1.8680 1681500 6024 0.6027 3.6386 288.73 42.76 17.054 2.2050 1985800 6017 0.6021 3.6362 287. 94 42.86 16.792 2. 1896 1975700 6014 0.6019

Table 18. Measured and Calculated Quantities Using Hater in the 3-Inch Orifice Meter,

0.73 Beta Ratio, 4.1 iim Roughness

Pipe Diameter = 7.813 cm Orifice Diameter • 5 7132 cm

Run ID Temperature Dif Press Flow Rate Pipe C (K) (kPa) (kg/s) Reynolds No. 06/26/87- 1 301.40 2.573 4.242 83258 0.61603 06/26/87- 2 301 . 45 2.588 4 .256 83628 0.61635 06/26/87- 3 301.52 2.596 4.261 83860 .61621 06/26/87- 4 301 .58 6.968 6.948 136907 0.61323 06/26/87- 5 301.61 7.023 6.978 137583 0.61346 06/26/87- 6 301.65 7.021 6.976 137657 0.61335 06/26/87- 7 301.71 21. 106 12.043 237954 0.61073 06/26/87- 8 301. 72 21.391 12. 127 239645 0.61083 06/26/87- 9 301.75 21.207 12.068 238645 .61052 06/26/87-10 301. 81 21. 122 12.052 238678 0.61095 06/26/87-11 301.83 21. 106 12.045 238642 .61082 06/26/87-12 301. 86 20.928 11.998 237854 0.61101 06/26/87-13 301. 89 69.536 21.788 432206 0.60871 06/26/87-14 301. 89 69.214 21.739 431241 0.60877 06/26/87-15 301.89 69.179 21.731 431082 0.60870 06/26/87-16 301.97 192.651 36.182 718961 0.60732 06/26/87-17 301.98 192.441 36. 169 718863 0.60744 06/26/87-18 301.98 192.630 36. 182 719124 0.60737 06/29/87-19 299.80 2.541 4.216 79898 0.61607 06/29/87-20 299.85 2.531 4 .210 79867 0.61635 06/29/87-21 299.91 2. 544 4.222 80198 0.61651 06/29/87-22 300 . 00 6.984 6.965 132570 .61390 06/29/87-23 300.04 7.057 7.001 133367 0.61384 06/29/87-24 300.07 7.070 7.007 133569 0. 61384 06/29/87-25 300 .27 21. 165 12.064 231013 0. 61084 06/29/87-26 300 .29 21.098 12.050 230846 0.61111 06/29/87-27 300.31 21.175 12.071 231338 0.61102 06/29/87-28 300.38 21. 184 12.077 231798 0.61120 06/29/87-29 300.40 21.308 12.112 232568 0.61118 06/29/87-30 300.41 21. 100 12.055 231531 .61131 06/29/87-31 300 .47 69.234 21.748 418228 0.60883 06/29/87-32 300. 49 69. 126 21. 736 418177 0.60897 06/29/87-33 300.52 69.415 21. 785 419388 0.60907 06/29/87-34 300.59 192.838 36.227 698615 0.60769 06/29/87-35 300.59 192.595 36.207 698235 0.60774 06/29/87-36 300.57 192.957 36.227 698316 0.60750

38

MM ^^^^m
Table 19. Measured and Calculated Quantities Using nitrogen Gas In the 3-Inch Orifice

Meter, 0.73 Beta Ratio, 4.1 pa Roughness

Run ID

36031087- 1 36031087- 2 36031087- 3 36031087- 4 36031087- 5 36031087- 6 36031087- 7 36031087- 8 36031787- 1 36031787- 2 36031787- 3 36031787- 4 36031787- 5 36031787- 6 36110987- 1 36110987- 2 36110987- 3 36110987- 4 36110987- 5 36110987- 6 36110987- 7 36110987- 8 36111087- 1 36111087- 2 36111087- 3 36111087- 4 36111087- 5 36111087- 6 36111087- 7 36111087- 8

Table 20

Pipe Di ameter 7.813 cm Orifice Diameter = 5.7132 cm

Pressure Temperature Density Dif Press Flow Rate Pipe c CY 2 (MPa) (K) (kg/m 3

) (kPa) (kg/s) Reynolds No 4.0521 288.23 47. 73 2.434 0.8913 799900 6097 0.6097

4 .0318 288.20 47.50 2.432 .8860 795500 6078 0.6078 4.0398 288.26 47.58 2.431 0. 8874 796500 6083 0.6084 3.9315 287.55 46.42 9.197 1. 7013 1531600 6068 0.6070 3.9319 286.70 46.58 9.152 1.6947 1528800 6049 0.6051 3.9310 287.38 46.45 9. 164 1.6940 1525700 6051 0.6053 3.6634 285.50 43. 59 19.762 2.4059 2183900 6039 0.6044 3.6650 287.49 43.28 19.728 2.3920 2160700 6031 0.6036

4 .0674 288.84 47 .80 2.736 0.9455 847200 6096 0.6096

4 .0709 288.76 47.86 2.700 0.9412 843500 6105 .6105 3.7199 284 .38 44 . 46 17. 746 2.2947 2087200 6019 0.6024

3. 7180 285.20 44 .29 17.810 2.2925 2081100 6014 0.6018 3.8986 289.48 45. 70 9.800 1.7307 1551500 6027 0.6029 3.9381 288.89 46.27 9.819 1.7491 1569400 6047 0.6050 3.7108 289.63 43.46 16.566 2.1947 1971200 6025 0.6029 3.7205 289.47 43.61 16.477 2.1914 1968800 6023 0.6027 3.8271 289. 49 44.85 12.401 1.9306 1732200 6032 0.6035 3.8218 288.52 44. 96 12.295 1.9235 1730000 6029 0.6031 4.0578 288. 12 47. 82 2.576 0.9152 821600 6079 .6079 4.0323 288.17 47 . 51 2. 586 0.9147 821300 6084 0.6084 3.9199 287.58 46.28 6.535 1.4287 1286400 6055 0.6056 3.9261 287.57 46.36 6.499 1.4254 1283400 6053 0.6054

4 .0037 288.83 47.05 2. 844 0.9535 855000 6076 0.6077 3.9954 288.81 46.96 2.838 0.9524 854300 6082 0.6083

3. 7776 287 .81 44 .56 11.797 1.8757 1690800 6026 0.6031 3.7767 287.54 44 . 59 11.640 1.8610 1678700 6019 0.6022 3.6454 288.93 42.81 17.111 2.2094 1989300 6014 0.6018 3.6549 284.12 43.72 16.901 2.2184 2020800 6013 0.6017 3.8914 287.34 45.99 6.388 1.4094 1270200 6061 0.6063 3.8813 287.96 45.76 6.528 1.4169 1275200 6043 0.6044

Measured and Calculated Quantities Using Hater in the 3-Inch Orifice Meter, 0.73 Beta Ratio, 7 . 6 fim Roughness

Pipe Diameter - 7.811 cm Orifice Diameter = 5 7132 cm

Run ID Temperature Dif Press Flow Rate Pipe C

(K) (kPa) (kg/s) Reynolds No. 07/14/87- 1 303. 10 2. 516 4. 195 85417 0.61606 07/14/87- 2 303. 13 2.541 4 .217 85937 0.61635 07/14/87- 3 303 . 16 2.519 4.202 85672 0.61673 07/14/87- 4 303.23 7.016 6.981 142583 0.61400 07/14/87- 5 303 .24 7.007 6.977 142524 0.61399 07/14/87- 6 303 .26 7.019 6.982 142688 0.61390 07/14/87- 7 303.30 20.970 12.023 245915 0.61162 07/14/87- 8 303 .32 21.005 12.029 246147 0.61144 07/14/87- 9 303.33 20.943 12.013 245873 0.61153 07/14/87-10 303.38 20.950 12.018 246213 0.61165 07/14/87-11 303.39 20.879 12.000 245898 0.61178 07/14/87-12 303.40 20.402 11.863 243143 0.61183 07/14/87-13 303. 43 69.207 21.796 447005 0.61034 07/14/87-14 303.43 69.304 21.807 447242 0.61024 07/14/87-15 303.43 69.337 21.815 447396 0.61030 07/14/87-16 303.53 193.177 36.379 747642 0.60976 07/14/87-17 303.53 193.011 36.367 747386 0.60981 07/14/87-18 303.54 192. 869 36.360 747404 0. 60992 07/15/87-19 302.89 2.544 4.226 85689 0.61717 07/15/87-20 302.93 2.532 4.217 85570 0.61732 07/15/87-21 302.96 2.534 4.220 85685 0.61756 07/15/87-22 303.07 6.993 6.975 141948 0.61438 07/15/87-23 303.08 6. 969 6.960 141686 0.61419 07/15/87-24 303 . 11 6.953 6.955 141657 0.61439 07/15/87-25 303 . 18 20 .830 11.988 244525 0.61185 07/15/87-26 303 . 19 20.791 11.971 244242 0.61159 07/15/87-27 303. 19 20.738 11.962 244096 .61187 07/15/87-28 303 .27 20.739 11.962 244518 0.61190 07/15/87-29 303.28 20.654 11.939 244087 0.61196 07/15/87-30 303.30 20.698 11.952 244455 0.61199 07/15/87-31 303. 58 69.267 21.803 448545 0.61029 07/15/87-32 303.59 69.333 21.823 449058 0.61057 07/15/87-33 303.62 69.280 21.806 448983 0.61032 07/15/87-34 303.64 68. 892 21.743 447881 0. 61029 07/15/87-35 303.66 69.070 21.774 448698 0.61036 07/15/87-36 303.68 69.064 21.774 448878 0.61038 07/15/87-37 303. 76 192.866 36.360 750977 0.60995 07/15/87-38 303.75 192.445 36.315 749888 0.60985 07/15/87-39 303.75 193.222 36.391 751453 0.60990

39
Table 21. Measured and Calculated Quantities using litiogen Gas in the 3-Inch Orifice

Meter, 0.73 Beta Ratio, 7.6 M» Roughness

Pipe Diameter = 7.811 cm Orifice Diameter = 5.7132 cm

Run ID Pressure Temperature Density

(kg/m3

) Dif Press Flow Rate Pipe c CY 2 (MPa) (K) (kPa) (kg/s) Reynolds No 36031287- 1 3. 9148 286. 86 46.35 9. 166 1.7085 1541700 6107 0.6109 36031287- 2 3 .9157 286.36 46.45 9. 109 1.7022 1537900 6097 0.6099 36031287- 3 3.6973 288.33 43. 52 18.586 2.3504 2116900 6086 0.6091 36031287- 4 3.6975 288.78 43. 45 18.470 2.3376 2105100 6077 0.6082 36031287- 6 4 . 1506 288.52 48.84 2.814 0.9735 872500 6120 0.6121 36032687- 1 3.6969 284 .79 44 . 11 18.442 2.3581 2144300 6089 0.6094 36032687- 2 3.6791 283 .74 44 . 08 18. 196 2.3393 2133200 6084 0.6089 36032687- 3 4 . 1043 288.45 48.31 2.694 0. 9490 851100 6131 0.6132 36032687- 4 4 .0921 288. 51 48. 15 2.700 0.9510 853000 6147 0.6148 36032687- 5 3 .9983 287 .45 47 .24 6.432 1.4514 1306500 6136 .6137 36032687- 6 4 .0082 287 .96 47.26 6.390 1.4461 1300000 6132 0.6133 36032687- 7 3.8735 287 .64 45.72 11.362 1.8925 1705400 6117 0.6119 36032687- 8 3. 8753 287 .29 45. 80 11.322 1.8900 1704500 6114 0.6117 36110487- 1 3. 7007 286.96 43 .79 12.443 1.9177 1734400 6052 0.6055 36110487- 2 3.7076 287.31 43.81 12.533 1.9301 1744000 6068 0.6071 36110487- 3 3 .7001 287.27 43 .73 12.478 1.9232 1738000 6065 0.6068 36110487- 4 3 .8130 287.53 45.02 6. 824 1. 4465 1304700 6081 0.6083 36110487- 5 3 .8053 287.64 44 .91 6. 893 1.4499 1307500 6072 0.6074 36110487- 6 3.8640 288.41 45.47 2.712 0. 9173 825100 6087 0.6088 36110487- 7 3.8751 288.44 45.60 2.672 0.9111 819400 6083 0.6083 36110487- 8 3.6278 288.04 42. 75 16.578 2. 1907 1977800 6061 0.606f. 36110487- 9 3.6291 283 . 83 43.46 16. 182 2. 1820 1990300 6061 0.6065 36110587- 1 3. 8903 287.24 45.99 7. 019 1.4847 1338800 6089 0.6090 36110587- 2 3.8494 287 .24 45.51 7.064 1. 4808 1336000 6086 0.6087 36110587- 3 3 . 7731 286.83 44 . 67 12.019 1.9091 1725600 6070 0.6073 36110587- 4 3. 7923 287. 13 44 . 65 12.053 1. 9136 1728000 6063 0.6066 36110587- 5 4 .0277 288. 12 47.46 2. 767 0. 9467 850500 6088 0.6089 36110587- 6 4 . 0294 288.22 47.46 2. 761 0.9493 852600 6112 0.6113 36110587- 7 4.0236 288.27 47.39 2.762 0.9478 851200 6106 . 6107 36110587- 8 3 .6737 288.21 43.26 16. 519 2.2049 1988700 6075 0.6079 36110587- 9 3.6888 288.22 43.44 16.193 2. 1866 1971800 6072 0.6077 36101686- 1 3 .9275 288.09 46.28 9.055 1.7025 1531500 6127 0.6129 36101686- 2 3.9268 288.46 46.21 9.055 1.6971 1525300 6112 0.6114 36101686- 3 3.6728 285.42 43. 71 20.150 2.4630 2236900 6111 0.6117 36101586- 4 3.6735 283.96 43.97 19.906 2.4499 2232900 6098 0.6103 36101686- 5 4 .0229 288.67 47 .31 2.620 0.9208 826200 6097 0.6097 36101686- 6 4 .0278 288.98 47.31 2.682 0.9316 835300 6096 0.6097 36102186- 1 3.9843 291.27 46. 39 8.646 1.6565 1477800 6093 0.6095 36102186- 2 3 . 9820 290.30 46.53 8.602 1.6547 1479700 6093 0.6095 36102186- 3 4 .0718 290.97 47 . 46 2.472 0.8991 801900 6117 0.6118 36102186- 4 4 . 0563 290.07 47.45 2. 465 0.8961 801100 6107 0.6108 36102186- 5 3 . 7099 282.58 44 .65 19. 429 2.4376 2228400 6096 .6101 36102186- 6 3.7088 285.94 44 . 06 19.508 2.4221 2195900 6084 0.6089

40
Table 22. Measured and Calculated Quantities Using Hitrogen Gas in the 4-Inch Orifice

Meter, 0.43 Beta Ratio, 0.76 ) Roughness

Run ID

43071886- 1 43071886- 3 43071886- 4 43071886- 5 43071886- 6 43072986- 1 43072986- 2 43072986- 3 43072986- 4 43072986- 5 43072986- 6 43080186- 1 43080186- 2 43080186- 4 43080186- 5 43080186- 6 43012188- 1 43012188- 2 43012188- 3 43012188- 4 43012188- 5 43012188- 6 43012188- 7 43012188- 8 43012188- 9 43020488- 1 43020488- 2 43020488- 3 43020488- 4 43020488- 5 43020488- 6 43020488- 7 43020488- 8

Table 23

Pipe Diameter = 10.368 cm Orifice Diameter = 4.4445 cm

Pressure Temperature Density Dif Press Flow Rate Pipe c CY 2 (MPa) (K) (kg/m 3

) (kPa) tkg/s) Reynolds No

4 . 0736 290. 36 47.59 3. 129 0.5219 351100 6061 0.6062

3. 7245 288.96 43.74 49.425 1. 9767 1339900 6007 0.6024 3.7241 288.81 43. 76 48. 820 1. 9613 1330000 5997 0.6013 3.8892 289.26 45.63 19.313 1.2599 851800 6008 0. 6015

3 .8880 289.29 45. 60 19.688 1.2732 860700 6015 0.6021

3 . 7847 288.36 44 . 55 47.704 1.9585 1328500 6004 .6020

3. 7842 288.36 44 .54 47 . 476 1.9528 1324700 6001 .6017

4 . 0664 289.91 47.59 3.003 0. 5106 343900 6054 .6055

4 . 0964 290.29 47. 87 2.991 0.5116 344200 6061 0.6062

3. 9354 288. 76 46.26 19.243 1.2700 859100 6026 0.6032 3.9356 288.72 46.27 19.081 1.2650 855900 6026 0.6034 3.9650 288.56 46.64 18.392 1.2472 843900 6029 0.6035 3.9650 288.41 46.67 18.363 1.2459 843200 6026 0.6032

4. 1115 289.52 48. 19 3.473 0.5511 371400 6039 0.6040

3. 8213 288.32 44 . 99 48.545 1.9913 1350400 6022 0.6038 3.8216 288. 14 45.02 48.333 1.9831 1345400 6008 0.6024

4 .0198 286.63 47.27 12.547 1.0331 698400 6008 0. 6011

4 .0089 288.74 47. 13 12.556 1. 0362 700400 6032 0.6036

4 . 0151 288.67 47 .21 12.551 1. 0363 700500 6029 0.6033

3 .8663 288. 09 45.56 28. 419 1.5275 1035800 6006 .6015

3 . 8710 288. 13 45. 61 28. 007 1.5167 1028300 6004 .6013

4 . 1118 289.29 48.24 4 . 350 0. 6187 417100 6053 0.6054

4 . 1343 289.33 48.50 4 .756 0.6498 437900 6062 0. 6064

3 .7778 287 .72 44 .58 48.528 1.9796 1345000 6015 0.6031

3 .7688 287 . 60 44.49 49. 010 1.9860 1349900 6010 0.6027 3.7767 288.44 44 . 44 49.327 1.9922 1351200 6012 0.6029 3.7781 288.36 44.47 49.196 1.9863 1347400 6001 0. 6018

4 . 0975 289.78 47.98 4.333 0.6116 411900 6010 .6011

4 . 1165 289.93 48. 18 4.879 0.6540 440200 6044 . 6045 3.9357 288. 84 46.25 27 .367 1.5181 1026700 6038 . 6047 3.9137 288.79 46.00 28. 043 1.5321 1036600 6036 0.6045

4 .0432 289.34 47 .42 13.227 1.0670 719900 6033 0.6037

4 . 0445 289.29 47.45 13 .373 1.0700 722000 6015 0.6019

Measured and Calculated Quantities Using Hitrogen Gas in the 4-Inch Orifice

Meter, 0.43 Beta Ratio, 3.8 itm Roughness

Pipe Dian- eter - 10.366 cm Orifice Diameter = 4.4445 cm

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe c CY 2 (MPa) (K) (kg/m 3

) (kPa) (kg/s) Reynolds No 43072386- 1 4 1317 288. 73 48. 58 3. 703 0.5731 386900 6057 0.6058 43072386- 2 4 1166 288.77 48.39 3.430 . 5490 370600 6040 0.6041 43072386- 3 3 9910 287.92 47 .07 18.442 1.2517 848100 6016 .6022 43072386- 4 3 9948 287 .86 47 . 12 18. 483 1.2533 849200 6013 .6019 43072386- 5 3 8380 287.28 45.36 49.536 2.0170 1371200 6013 . 6029 43072386- 6 3 8390 287 .43 45.35 49.035 1.9990 1358400 5991 0.6007 43072386- 7 3 8387 287.36 45.36 48.923 2.0028 1361300 6009 0.6025 43072486- 1 4 0088 287 . 73 47.31 17.820 1.2369 838200 6032 0.6038 43072486- 2 4 0081 287.75 47.30 17.866 1.2374 838600 6028 0.6033 43072486- 3 4 1653 288.66 48.99 3.349 0.5475 369500 6059 0.6060 43072486- 4 4 1627 288. 91 48.91 3.179 0.5336 359900 6067 0.6068 43072486- 5 3 8528 287 .76 45.46 47 . 933 1.9894 1350600 6023 .6039 43072486- 6 3 8535 287. 46 45.52 47.591 1.9793 1344800 6011 .6026 43073186- 1 4 0625 289. 97 47 . 54 3. 197 0.5260 354300 6047 . 6048 43073186- 3 3 7344 288. 11 43.99 50. 528 2.0100 1365400 6024 0.6041 43073186- 4 3 7345 288.28 43.97 49.997 1.9941 1354100 6010 0.6027 43073186- 5 3 8833 288. 73 45.65 20.484 1.2963 877700 6001 0.6007

41
Table 24. Measured and Calculated Quantities Using Nitrogen Gas in the 4-Inch Orifice

Meter, 0.43 Beta Ratio, 6.9 iim Roughness

Run ID

43072286- 1 43072286- 2 43072286- 3 43072286- 4 43072286- 5 43072286- 6 43072586- 1 43072586- 2 43072586- 3 43072586- 4 43072586- 5 43080586- 1 43080586- 2 43080586- 3 43080586- 4 43080586- 5 43080586- 6

Table 25.

Pice Diamet er = 10 . 378 cm Orifice Diameter = 4.444 5 cm

Pressure Temperature Density

(kg/m 3

) Dif Press Flow Rate Pipe c CY 2 (MPa) (K) (kPa) (kg/s) Reynolds N o . 3.9996 287 .93 47 . 16 17.766 1.2336 834700 6034 0.6040

3. 9990 287.93 47.16 17.714 1.2307 832700 6029 0. 6035

3 . 8380 287. 43 45.34 47 .456 1.9715 1338100 6007 0.6023

3. 8375 287.41 45.33 47 .072 1.9617 1331500 6002 0.6018

4. 1268 288. 71 48. 52 3.264 0. 5375 362400 6054 0.6055

4 . 1307 288. 69 48.57 3 . 916 . 5882 396700 6046 0. 6047

3 .8296 287.68 45. 20 46. 843 1.9558 1326800 6008 0.6024

3 .8293 287 .51 45.22 46. 645 1.9495 1323100 6000 0.6015 3.9688 287 .78 46. 83 20.359 1.3101 887100 6007 0.6014 3.9679 287 . 84 46. 80 20.528 1.3160 890900 6010 .6017

4 . 1648 288.87 48.94 2. 895 . 5068 341500 6040 . 6041

3 .9463 288. 13 46.50 19. 464 1.2802 866300 6025 0.6031

3.9457 288. 17 46 . 48 19. 551 1.2799 866100 6011 0. 6018

4 . 1434 289.25 48.62 3.121 0. 5255 353800 6054 0.6054

4. 1093 289.34 48.20 3.063 0.5181 348900 6048 0.6049

3. 8034 287.48 44 .92 50.328 2. 0209 1372100 6006 0.6023

3 . 8031 287. 73 44 .87 49.976 2. 0090 1363200 5995 0.6012

Measured and Calculated Quantities Using Water in the 4-Inch Orifice Meter, 0.55 Beta Ratio, 0.76 iim Roughness

Pipe Diameter = 10.368 cm Orifice Diameter = 5.7137

Run ID

03/19/87-

03/19/87-

03/19/87-

03/19/87-

03/19/87-

03/19/87-

03/19/87-

03/19/87- 8 03/19/87- 9 03/19/87-10

03/20/87-11

03/20/87-12

03/20/87-13

03/20/87-14

03/20/87-15

03/20/87-16

03/20/87-17

03/20/87-18

03/20/87-19

03/20/87-20

Temperature

(K) 301. 18 301.23 301.32

301. 34 301.41

301.43

301.47

301.48

301. 58 301. 59 302. 56

302. 61 302. 70 302. 71 302.79

302.80

302.84

302. 85 302.88

302. 89

Dif Press Flow Rate

(kPa) 2.545

2.522

20. 791 20.785

21.033

21. 173 69.627 69.475

193. 140

192. 893

554

527 21.242 21.451

21.034

21. 178 69.057 69.246

192.659

192.984

(kg/s) 3.699

3.684 10.526

10.521

10. 590 10.627 19.221

19.197

31. 967

31. 939

3. 709 3.691

10.641 10.692

10. 590 10.627

19. 136

19. 165 31.918

31.945

Pipe

Reynolds No. 54454 54289 155409

155437 156698

157304 284772

284470

474706

474387

56248

56033 161895

162700 161415

162010 291976

292469

487403 487927

60888

60913

60620

60601

.60642 60650

. 60495

.60484 .60408

.60393 .60951

. 60982

.60645

. 60636

.60649

. 60654 0.60484 0.60491

0.60399

0.60400

Table 26. Measured and Calculated Quantities Using Bitrogen Gas in the 4-Inch Orifice

Meter, 0.55 Beta Ratio, 0.76 iim Roughness

Pipe Diame ter = 10.368 cm Orifice Diameter = 5.7137 cm

Run ID Pressure Temperature Density

(kg/m 3

) Dif Press Flow Rate Pipe c CY 2 (MPa) (K) (kPa) (kg/s) Reynolds No 44062587- 1 3.8646 289.27 45.33 15.000 1. 8803 1271500 .5987 0. 5992 44062587- 2 3.8704 288.62 45.51 14.888 1.8815 1274300 6002 0.6007 44062587- 3 4.0973 287.03 48.49 2.741 0.8355 566500 6023 0.6024 44062587- 4 4.0938 288.61 48. 15 2.666 0.8224 555500 6032 0.6033 44062587- 5 3. 7055 291. 18 43.15 23 .988 2.3231 1566700 5992 0.6000 44062587- 6 3.7143 287.31 43.89 23.466 2.3147 1575500 5987 0.5994 44062587- 7 3.9626 286.56 46. 97 7.650 1.3738 934000 6021 0.6023 44062587- 8 3.9759 288. 10 46. 85 7. 735 1.3772 932700 6010 0.6012 44012188- 1 4 . 0718 288.75 47. 87 2.990 0. 8722 589100 6059 0.6060 44012188- 2 4 .0443 288.86 47.52 2.979 0.8687 586700 6067 0.6068 44012188- 3 3 . 9390 288.23 46.39 7.254 1.3360 904800 6050 0.6052 44012188- 4 3.9179 288.24 46. 14 7.147 1.3219 895500 6047 0.6050 44012188- 5 3.6833 287. 12 43.55 22.292 2.2586 1538500 6017 0.6024 44012188- 6 3.6774 286. 77 43.54 22.067 2.2442 1530100 6010 0.6017 44012188- 7 3.8286 287.56 45.20 15.640 1.9238 1306700 6008 0.6013 44012188- 8 3.7995 287.28 44 . 91 15.655 1.9182 1304300 6008 0.6013 44012888- 1 4 .0936 288. 42 48. 18 2.669 0.8262 558300 6054 0.6055 44012888- 2 4 .0993 288. 43 48.25 2.731 0. 8366 565200 6057 0.6057 44012888- 3 3 . 7182 288.45 43. 75 22.382 2.2668 1538500 6013 0.6020 44012888- 4 3 . 7092 288.53 43.63 22.050 2.2472 1525100 6014 0.6021

44012888- 5 3. 9359 289. 13 46.20 8. 083 1. 4097 952700 6060 0.6062 44012888- 6 3.9378 289.24 46.20 8. 153 1.4130 954700 6048 0.6051 44012888- 7 3.9379 289. 34 46. 18 8. 131 1.4114 953300 6050 0.6053 44012888- 8 3.8460 288.74 45.20 14.248 1.8394 1245600 6019 0.6023 44012888- 9 3.8506 289. 11 45.20 14 . 163 1.8322 1239600 6014 0. 6018

42
Table 27. Measured and Calculated Quantities Using Hater in the 4-Inch Orifice Meter, 0.55 Beta Ratio, 3 . 8 fim Roughness

Pipe Diameter - 10.366 cm Orifice Diameter 5

.

7137 cm

Run ID Temperature Dif Press Flow Rate Pipe C

(K) (kPa) (kg/s) Reynolds No . 03/17/87- 1 299.81 2.523 3.687 52683 0.60942 03/17/87- 2 299.87 2.549 3. 708 53042 0.60976 03/17/87- 3 300. 13 20.930 10.563 152004 0.60623 03/17/87- 4 300. 15 20.898 10.558 151998 0.60641 03/17/87- 5 300.24 20.861 10.553 152227 0.60670 03/17/87- 6 300.27 20 . 758 10.526 151938 0.60665 03/17/87- 7 300.30 69.084 19. 156 276663 0.60513 03/17/87- 8 300.32 69.082 19. 155 276781 0.60514 03/17/87- 9 300.37 192.768 31.948 462124 0.60420 03/17/87-10 300.38 192.984 31.957 462354 0.60403 03/18/87-11 301. 71 2.530 3.693 54998 0.60971 03/18/87-12 301.75 2.566 3. 718 55411 0.60947 03/18/87-13 301.82 20. 999 10.580 157969 0.60632 03/18/87-14 301.83 20.960 10. 564 157763 0.60597 03/18/87-15 301.92 20.889 10. 556 157947 0.60656 03/18/87-16 301. 94 20.907 10.560 158071 0.60652 03/18/87-17 301.96 69.539 19.207 287626 0.60489 03/18/87-18 301. 97 69. 541 19.213 287773 0. 60506 03/18/87-19 301 .99 192.607 31.916 478252 0.60396 03/18/87-20 301 . 99 192.637 31.918 478279 0.60394

Table 28. Measured and calculated quantitites using Hitr<>gen Gas in the 4-Inch Ori

Run ID

44082086- 1 44082086- 2 44082086- 3 44082086- 4 44082086- 5 44082086- 6 44062687- 1 44062687- 2 44062687- 5 44062687- 6 44062687- 7 44062687- 8

Pipe Diame ter « 10.366 cm Orifice Diameter » 5.7137 cm

ressure Temperature Density

(kg/m 3

) Dif Press Flow Rate Pipe c CY 2 (MPa) (K) (kPa) (kg/s) Reynolds No

3 .9906 287.26 47. 18 8.942 1. 4902 1011300 6027 0.6030

3 . 9890 287.27 47. 16 8.912 1.4876 1009500 6028 .6031

4 . 1199 287 . 74 48.62 2.473 0.7974 539700 6044 0.6045

4 . 1307 287 .68 48. 76 2.443 0. 7921 536100 6031 0.6032 3.7333 286. 70 44.22 24 .983 2. 4156 1646600 6032 0.6040 3.7242 286.71 44 . 11 24 . 547 2.3839 1625100 6013 0.6021

3. 8786 286. 48 45.99 14 .855 1.8915 1287700 6010 0.6014 3.8785 286.72 45.94 14 .798 1.8871 1284000 6010 .6015

4 .0509 289.34 47.51 4 .288 1.0387 700900 6047 0.6048 4.0523 289. 38 47.52 4 .277 1.0371 699700 6044 0.6046 3.7461 288. 85 44 .01 22.762 2.2913 1553500 6009 0.6016 3.7372 288. 49 43. 96 22.629 2.2827 1549100 6007 0.6014 44062687-10 4 .0423 293.23 46.72 2.966 0.8575 573400 6053 0.6054

Table 29. Measured and Calculated Quantities Dsing Hater in the 4-Inch Orifice Meter, 0.55 Beta Ratio, 6.9 pa Roughness

Pipe Diameter « 10.378 cm Orifice Diameter 5 7137 cm

Run ID Temperature Dif Press Flow Rate Pipe C

(K) (kPa) (kg/s) Reynolds No. 03/12/87- 1 299.08 2.510 3 .684 51719 0.61060 03/12/87- 2 299. 12 2. 509 3 .684 51766 0.61079 03/12/87- 5 299.37 20. 642 10.498 148337 0.60678 03/12/87- 6 299.38 20.624 10.493 148301 0.60676 03/12/87- 7 299. 55 69.590 19.232 272880 0.60544 03/12/87- 8 299. 58 69. 568 19.234 273078 0.60559 03/12/87- 9 299.63 192.586 31.954 454173 0.60469 03/12/87-10 299.64 192.552 31.959 454349 0.60485 03/16/87-11 299.92 2.548 3.708 53040 0.61008 03/16/87-12 299.97 2.503 3.677 52651 0.61033 03/16/87-13 300.03 2.523 3.692 52935 0.61043 03/16/87-14 300.07 2.515 3.687 52916 0.61059 03/16/87-15 300. 15 20. 777 10.528 151383 0.60661 03/16/87-16 300. 17 20.745 10.521 151355 0.60670 03/16/87-17 300.08 20.644 10.501 150733 0.60698 03/16/87-18 300. 14 20. 402 10.438 150061 0.60694 03/16/87-19 300.22 69.285 19.189 276337 0.60546 03/16/87-20 300.26 68. 713 19.107 275390 0.60538 03/16/87-21 300.35 193.004 31.983 461867 0.60464 03/16/87-22 300.35 193.277 32.009 462239 0.60470

43
Table 30. Measured and Calculated Quantities Using nitrogen Gas in the 4-Inch Orifice

Meter, 0.55 Beta Ratio, 6.9 iim Roughness

Run ID

44051387- 1 44051387- 2 44051387- 4 44051387- 5 44051387- 7 44051387- 8 44051587- 3 44051587- 4 44051587- 5 44051587- 6 44051587- 7 44051587- a 44062487- 1 44062487- 2 44062487- 3 44062487- 4 44062487- 5 44062487- 6 44062487- 7

Table 31.

Pipe Di ameter = 10.378 cm Orifice Diameter = 5.7137 cm

Pressure Temperature Density Dif Press Flow Rate Pipe c CY 2 (MPa) (K) (kg/m 3

) (kPa) (kg/s) Reynolds No

3 .9310 288.38 46.27 7. 340 1.3387 905600 6036 0.6038 3.9468 288.62 46.42 7.358 1.3420 907100 6034 .6036 3.7112 288.77 43.61 23 .013 2.2936 1554100 6010 .6018 4.0685 288.62 47 .85 3. 121 . 8924 602400 6070 .6071 3.8902 286. 53 46. 12 14.927 1. 9044 1294600 6029 0.6034 3.8881 289. 60 45.55 15.050 1. 8999 1282000 6026 0.6031 3.7089 287 . 49 43 . 80 23. 853 2. 3471 1595300 6029 0.6036

3.7141 288. 13 43. 75 23. 867 2.3447 1591000 6023 .6031

4 .0959 287 . 59 48.37 2.846 0. 8544 577900 6053 0.6054

4 .0911 287 . 64 48. 30 2. 833 0.8530 576900 6061 .6062 3.8962 289. 59 45.65 14. 785 1. 8869 1273200 6033 0. 6037

3. 9157 289. 96 45. 82 14. 773 1.8863 1271400 6022 0. 6026

3. 7043 287 .23 43. 78 23.311 2.3213 1578800 6032 . 6040

3. 7115 288. 01 43. 74 23.351 2.3231 1576900 6035 0. 6042 3.8584 288. 13 45. 46 14.871 1. 8925 1282100 6046 . 6050 3.9528 287 .31 46. 72 7.651 1.3800 935600 6065 . 6067 3.7250 286.40 44. 17 22. 700 2.3020 1568500 6036 0. 6043

3. 8617 285.07 46.04 14 . 911 1.9060 1300800 6043 . 6048 3.9561 286. 10 46. 98 7.641 1.3789 937600 6047 0.6050

Measured and Calculated Quantities using Water in the 4-Inch Orifice Meter,

0.67 Beta Ratio, 0.76 fim Roughness

Pipe Diameter = 4.082 cm Orifice Diameter = 6 9840 cm

Run ID Temperature Dif Press Flow Rate Pipe C

(K) (kPa) (kg/s) Reynolds No. 03/19/87- 1 301.85 2.521 5.931 88603 0.61420 03/19/87- 2 301. 88 2. 519 5. 931 88654 . 61438 03/19/87- 3 301.96 21. 338 17.106 256114 . 60881 03/19/87- 4 301. 98 21.281 17 .083 255887 0.60883 03/19/87- 5 302.04 21.080 17.012 255137 0.60917 03/19/87- 6 302. 05 21.304 17. 109 256659 0. 60945 03/19/87- 7 302.04 68. 708 30.611 459103 0. 60716 03/19/87- 8 302.04 68. 523 30 . 562 458359 0. 60700 03/19/87- 9 302.07 192.383 51.099 766854 0.60570 03/19/87-10 302.07 192.383 51. 106 766971 0. 60579 03/20/87-11 302.23 2.529 5. 935 89386 0. 61357 03/20/87-12 302.27 2.529 5. 936 89470 0. 61361 03/20/87-13 302. 35 21.226 17.058 257564 0. 60877 03/20/87-14 302. 37 21.244 17 . 062 257732 0. 60864 03/20/87-15 302.43 21.250 17.084 258390 0.60935 03/20/87-16 302.44 21.039 16.989 257008 . 60899 03/20/87-17 302.45 69.297 30. 741 465138 0. 60718 03/20/87-18 302. 46 69.557 30 . 804 466181 0. 60728 03/20/87-19 302. 49 192. 449 51. 105 773908 0. 60570 03/20/87-20 302.48 192.462 51. 110 773811 0. 60573

Table 32. Measured and Calculated Quantities Using nitrogen Gas in the 4-Inch Orifice

Meter, 0.67 Beta Ratio, 0.76 iim Roughness

Pipe Diame ter =- 10.368 cm Orifice Diameter = 6.9840 cm

Run ID Pressure Temperature Density

(kg/m 3

) Dif Press Flow Rate Pipe c CY 2 (MPa) CK) (kPa) (kg/s) Reynolds No 45062587- 1 3. 8891 287.74 45. 89 6.715 2.0405 1384600 .6046 . 6047 45062587- 2 3.8923 288. 16 45. 85 6. 703 2.0366 1380400 .6042 0. 6044 45062587- 3 4.0134 288. 41 47 .24 2. 808 1.3411 907200 .6058 0.6058 45062587- 4 4 .0072 288.39 47 . 17 2.794 1.3419 907800 6080 0.6081 45062587- 5 3 . 7444 287.27 44.25 9. 137 2.3317 1586700 6030 0.6033 45062587- 6 3. 7552 288.04 44.25 9. 195 2.3373 1587300 6026 . 6028 45062587- 7 3.9079 287.63 46. 13 5.185 1.7969 1219300 6043 0.6045 45062587- 8 3 . 8997 287 .81 46.00 5.206 1. 7941 1217000 6030 0.6032 45012788- 1 3.8702 288. 73 45. 49 5.107 1.7640 1194300 6020 0.6021 45012788- 2 3 .8662 288.78 45.44 5.080 1. 7590 1190800 6022 0.6024 45012788- 3 3. 6855 288.28 43.39 8.520 2.2197 1507700 6004 0. 6006 45012788- 4 3 . 6828 287.62 43. 47 8.453 2.2140 1506300 6007 . 6009 45012788- 5 3. 8279 288. 51 45.03 6.280 1. 9430 1316800 6009 0. 6011 45012788- 6 3 . 8167 288.42 44 .91 6.290 1.9456 1319000 6021 0.6022 45012788- 7 3. 9297 289. 18 46. 12 2. 548 1.2592 851000 6043 0. 6043 45012788- 8 3.9202 289.24 45. 99 2. 522 1.2519 846000 6047 .6048 45020488- 1 3.9712 289. 18 46. 60 2.754 1.3200 891600 6061 0.6062 45020488- 2 3 . 9663 289. 11 46. 56 2. 738 1.3169 889700 6067 0.6068 45020488- 3 3. 8423 288.37 45.22 6. 193 1.9377 1313400 6022 0.6024 45020488- 4 3. 8549 288.25 45.39 6.209 1.9451 1318600 6026 0.6028 45020488- 5 3 . 6901 288.01 43 . 49 8.868 2.2714 1543700 6015 0.6017 45020488- 6 3.6919 287.29 43.63 8.795 2.2651 1542100 6013 0.6016 45020488- 7 3. 8698 288.31 45. 56 5. 073 1.7612 1193600 6026 0.6027 45020488- 8 3 . 8555 288.43 45.37 5. 139 1. 7700 1199400 6029 .6031

44
Table 33. Measured and Calculated Quantities Using Hater in the 4-Inch Orifice Meter,

. 67 Beta Ratio , 3.8 iim Roughness

Pipe Diameter - 10.366 cm Orifice Diameter 6 9840 cm

Run ID Temperature Dif Press Flow Rate Pipe C

(K) (kPa) (kg/s) Reynolds No. 03/17/87- 1 300. 53 2.521 5.937 86188 0.61464 03/17/87- 2 300.56 2.518 5.934 86208 0.61477 03/17/87- 3 300. 67 20.756 16.890 245938 0.60936 03/17/87- 4 300.68 20.727 16.878 245808 .60935 03/17/87- 5 300. 72 20.807 16.926 246733 0.60994 03/17/87- 6 300. 75 20.600 16.840 245633 0.60986 03/17/87- 7 300.78 69.358 30.797 449500 0.60784 03/17/87- 8 300.79 69. 443 30.817 449892 0.60787 03/17/87- 9 300 .82 192.906 51.269 748934 0. 60675 03/17/87-10 300.83 195.208 51.556 753300 0.60655 03/17/87-11 300. 82 192.629 51.214 748142 .60654 03/17/87-12 300. 82 192. 474 51.218 748201 .60683 03/18/87-13 301.51 2.498 5.905 87573 0.61418 03/18/87-14 301.55 2.509 5. 920 87863 0.61436 03/18/87-15 301.62 20.920 16.954 252017 0. 60933 03/18/87-16 301.65 20.791 16.897 251324 . 60916 03/18/87-17 301. 69 21.064 17.016 253319 0.60949 03/18/87-18 301. 71 20. 969 16.987 252989 0.60981 03/18/87-19 301.71 69. 174 30. 742 457848 0.60763 03/18/87-20 301.71 68.988 30.698 457187 0.60757 03/18/87-21 301.74 192.807 51.224 763372 0.60644 03/18/87-22 301. 73 192.751 51.226 763249 0.60656

Table 34. Measured and Calculated Quantities Using Bitroj[en Gas in the 4-Inch Orif

Pipe Diamet er = 10 . 366 cm Orifice Diameter = 6.9840 cm

Run ID Pressure Temperature Density

(kg/m3

) Dif Press Flow Rate Pipe c CY 2 (MPa) (K) (kPa) (kg/s) Reynolds No. 45082086- 1 4.0073 287. 77 47.28 2. 570 1.2823 868900 6052 0.6053 45082086- 2 4 . 0055 287. 59 47.29 2.556 1.2814 868700 6063 0.6063 45082086- 3 3. 9813 287.69 46.99 5. 123 1.8085 1226100 6062 0.6063 45082086- 4 3.9800 286.78 47 . 14 5.139 1.8121 1231300 6056 0.6057 45082086- 5 3.7469 286.96 44 .34 9.573 2.3999 1634500 6057 0.6060 45082086- 6 3.7527 286.98 44. 40 9.487 2.3865 1625200 6047 . 6049 45082986- 1 3.9426 287.86 46.50 5.064 1.7806 1207200 6035 0.6036 45082986- 2 3.9424 287.73 46.52 5.069 1.7856 1211000 6047 0.6049 45082986- 3 4 .0134 287.73 47.36 2.612 1.2985 879900 6072 0.6072 45082986- 4 4 .0128 288.59 47.20 2.624 1.2954 876000 6054 0.6055 45082986- 5 3.7090 287. 06 43.87 10. 116 2.4473 1667200 6040 0.6043 45082986- 6 3.7108 287.37 43 .84 10.081 2.4443 1663900 6046 0.6049

Table 35. Measured and Calculated Quantities Using Hater in the 4-Inch Orifice Meter, 0.67 Beta Ratio, 6.9 itm Roughness

Pipe Diameter » 10.378 cm Orifice Diameter TM 6 9840 cm

Run ID Temperature Dif Press Flow Rate Pipe C

(K) (kPa) (kg/s) Reynolds No. 03/12/87- 2 299.81 2.554 5.978 85299 0.61524 03/12/87- 3 299.86 2.553 5.978 85392 0.61533 03/12/87- 6 299.99 20.923 16.966 243076 0.61000 03/12/87- 7 300.02 20.917 16.966 243240 0.61010 03/12/87-11 300. 14 21.070 17.034 244847 0.61033 03/12/87-12 300.15 20.982 17.001 244416 0.61040 03/12/87-13 300.17 69.408 30.840 443579 0.60882 03/12/87-14 300.19 69.428 30.850 443912 0.60893 03/12/87-15 300.29 192.450 51.291 739786 0.60809 03/12/87-16 300.29 192.872 51.364 740838 0.60828 03/13/87-19 300.39 2.491 5.894 85192 0.61418 03/13/87-20 300.42 2.542 5.951 86081 0.61389 03/13/87-21 300. 50 2.532 5.941 86078 0.61407 03/13/87-22 300. 54 2.544 5.956 86363 0.61411 03/13/87-23 300.59 21.406 17.146 248897 0.60952 03/13/87-24 300.60 21.290 17.107 248380 0.60979 03/13/87-25 300.63 21.402 17. 146 249160 0.60958 03/13/87-26 300.63 21.433 17. 160 249371 0.60965 03/13/87-27 300.69 21.281 17.111 248974 0.61007 03/13/87-28 300.70 21.101 17.036 247938 0.60999 03/13/87-29 300.77 69.260 30.782 448653 0.60836 03/13/87-30 300.78 69.250 30. 776 448669 0.60829 03/13/87-31 300.84 192.963 51.330 749267 0.60778 03/13/87-32 300.87 194.527 51.526 752604 0.60764

45
Table 36. Measured and Calculated Quantities Using Mitrogen Gas in the 4-Inch Orifice

Meter, 0.67 Beta Ratio, 6.9 turn Roughness

Pipe Di ameter = 10.378 cm Orifice Diameter = 6.9840 cm

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe c CY2 (MPa) (K) (kg/m 3

) tkPa) (kg/s) Reynolds No. 45051387- 1 3 9132 289. 53 45.86 4. 778 1. 7372 1172100 6107 6108 45051387- 2 3 9077 288. 91 45.91 4.758 1.7310 1169700 6095 6097 45051387- 3 3 7166 284.77 44 .35 9. 320 2.3741 1624200 6076 6079 45051387- 4 3 7166 285. 50 44 .23 9.333 2.3770 1623300 6088 6091 45051387- 5 3 9798 285.36 47.40 2.757 1.3348 909000 6079 6080 45051387- 6 3 9617 289.52 46.43 2.803 1.3403 903800 6114 6115 45051387- 7 3 9679 289.34 46.54 2. 801 1. 3389 903200 6104 6105 45051387- 8 3 8749 289. 48 45.42 6.608 2.0263 1367900 6086 6088 45051387- 9 3 8521 288. 94 45.24 6.566 2.0137 1361600 6080 6081 45051587- 3 3 7358 288.02 44.03 9.059 2. 3222 1575900 6050 6053 45051587- 4 3 9593 287.28 46.80 2.843 1.3397 908300 6046 6046 45051587- 5 3 9743 287 . 92 46.87 2.865 1.3525 915500 6075 6076 45051587- 6 3 9376 287 .28 46.55 4.531 1. 6931 1148300 6068 6069 45051587- 7 3 9544 287. 17 46.76 4 .536 1.6998 1152800 6074 6075 45051587- 8 3 8633 288. 08 45.52 6.725 2.0353 1378900 6053 6055 45051587- 9 3 8533 286.56 45.67 6.651 2.0297 1380300 6061 6062 45051587- 10 3 9807 287 . 55 47.01 2.623 1.2939 876500 6065 6066 45062487- 1 3 9151 288. 96 45.98 4 .396 1.6590 1120900 6072 6073 45062487- 2 3 9004 288. 89 45.82 4 .378 1.6528 1117100 6073 6075 45062487- 3 3 6979 284 . 51 44 . 17 9. 397 2.3654 1619700 6041 6044 45062487- 4 3 6941 285. 11 44 . 02 9.394 2.3658 1617700 6054 6056 45062487- 5 3 9809 285. 09 47.46 2. 584 1.2934 881300 6080 6080 45062487- 6 3 9661 285. 19 47.27 2. 581 1.2896 878700 6077 6078 45062487- 7 3 8419 287 . 96 45.29 6.723 2. 0359 1380000 6071 6073 45062487- 8 3 8444 288. 13 45.29 6. 723 2.0348 1378700 6068 6070

Table 37. Measured and Calculated Quantities Using Water in the 4-Inch Orifice Meter,

0.73 Beta Ratio, 0.76 iim Roughness

Pipe Diameter = 10.368 cm Orifice Diameter = 7 6177 cm

Run ID Temperature Dif Press Flow Rate Pipe C

(K) (kPa) (kg/s) Reynolds No. 03/19/87- 1 302. 16 2.531 7.481 112481 0.61383

03/19/87- 2 302. 19 2.523 7.466 112332 0.61358

03/19/87- 3 302.25 20.852 21.277 320581 0.60823

03/19/87- 4 302.27 20.804 21.259 320458 0.60845

03/19/87- 5 302.30 20.538 21.127 318667 0.60858

03/19/87- 6 302.33 21.178 21.454 323800 0.60858

03/19/87- 7 302.31 69.307 38.659 583220 0.60619

03/19/87- 8 302.30 69.304 38.657 583074 0.60618

03/19/87- 9 302.39 193.219 64 . 328 972104 0.60412

03/19/87- 10 302. 41 192. 550 64 .240 971183 0.60435

03/20/87- 11 301.60 2. 538 7. 497 111369 .61419 03/20/87- 12 301.65 2.529 7 .488 111353 0. 61452 03/20/87- 13 301.72 21.229 21.469 319761 0.60824

03/20/87- 14 301.74 21.281 21.488 320179 0.60804

03/20/87- 15 301. 78 21. 163 21. 454 320012 0.60877

03/20/87- 16 301.80 20.761 21.248 317058 0.60870

03/20/87- 17 301.83 68. 726 38.503 574908 0.60626

03/20/87- 18 301.84 68.630 38.472 574576 0.60620

03/20/87- 19 301. 94 192.573 64 .232 961315 0.60420

03/20/87- 20 302.00 192.652 64 .273 963145 0.60447

46
Table 38. Measured and Calculated Quantities Using litrogen Gaa in the 4-Inch Orifice Meter,

0.73 Beta Ratio, 0.76 ia Roughness

Pipe Diame ter - 10.368 cm Orifice

Dif Press

Diameter TM

Flow Rate

7.6177 cm

Pipe c

'

Run ID Pressure Temperature Density

<kg/m3

) CY 2 (MPa) (K) (kPa) (kg/s) Reynolds No 46071886- 1 3.9641 289.21 46.51 2.375 1.5326 1035400 6023 0.6024 46071886- 3 3.9408 289.24 46.23 2.353 1.5250 1030400 6039 0.6039 46071886- 4 3.8011 289.01 44.63 4.449 2.0477 1386600 6001 0.6002 46071886- 5 3.7938 288.90 44.56 4.442 2.0495 1388300 6015 0.6017 46071886- 6 3. 5840 287.56 42.31 6.482 2.4079 1640500 6005 0.6007 46071886- 7 3.5760 286.74 42.34 6.382 2.3917 1632800 6008 0.6010 46072986- 1 3.9262 289.06 46. 10 2.437 1.5484 1046800 6034 0.6035 46072986- 2 3.9252 288.93 46. 11 2.453 1.5571 1053000 6048 0.6048 46072986- 3 3.6464 288.22 42.94 6.425 2.4189 1644200 6014 0.6016 46072986- 4 3.6451 287.77 42.99 6.358 2. 4047 1636300 6006 . 6008 46072986- 5 3. 8038 288.31 44.78 4.418 2.0447 1386900 6003 0.6004 46072986- 6 3.8028 288.18 44. 79 4.454 2.0577 1396100 6016 0.6017 46080186- 3 3.6677 287.95 43.23 6.636 2.4718 1680800 6026 0.6028 46080186- 4 3.6674 287.91 43.24 6.566 2.4581 1671600 6025 0.6026 46080186- 5 3.9528 288.52 46. 50 2.451 1.5637 1058200 6049 0.6050 46080186- 6 3.9521 288.52 46. 50 2.478 1.5705 1062800 6043 0.6043 46012788- 1 3.6959 287.92 43.57 5.364 2.2226 1510900 6004 0.6006 46012788- 2 3. 6913 287.79 43.54 5.428 2.2391 1522600 6016 0.6017. 46012788- 3 3.8199 288.4 4 44.95 3.866 1.9178 1300100 6008 . 0.6009

46012788- 4 3 .8059 288.03 44.85 3.853 • 1.9119 1297600 6007 0.6008 46012788- 5 3. 8809 288.56 45.65 2.766 1.6379 1109200 6020 0.6021 46012788- 6 3. 8770 288.65 45.59 2. 781 1.6434^ i 1112800 e .6029 • 0.6029 46012788- 7 3. 7509 287.99 44.21 4 .677 2.0965 . 1423900 6022 0.6023 46012788- 8 3.7515 288.31 44. 16 4.679 : 2.0921 1419900 6011 0.6012

460,12888- 1 3.7667 288.54 44 .30 4 .660 2.0902 • 1417500 6008 0.6009 46012888- 2 3.7591 288.57 44.21 4 . 638 2.0807 1 1411100 .6001 0.6002 46012888- 3 3.8742 288.69 45.55 2.758 1.6330 \ 1105600 6019 0.6019 46012888- 4 3.8631 288.71 45.41 2.764 1.6337 ! 1106200 '6023 0.6023 46012888- 5 3.8129 288.61 44 . 84 3.710 1.8751 1270700 •6005 0.6006 46012888- 6 3. 8088 288.57 44. 80 3.694 1.8688 1266600 6000 0.6001 46012888- 7 3.6772 287.66 43.39 5.572 2.2632 1539700 6011 0.6012 46012888- 8 3.6822 288.26 43.35 5.579 2.2618 1536500 6006 0.6008

Table 39. Measured and Calculated Quantities using Hater in the 4-Inch Orifice Meter,

0.73 Beta Ratio, 3 . 3 turn Roughness

Pipe Diameter 10.366 cm Orifice Diameter TM 7 6177 cm

Run ID Temperature Dif Press Flow Rate Pipe C (K) (kPa) (kg/s) Reynolds No. 03/17/87- 1 301.11 2.544 7.516 110499 0.61492 03/17/87- 2 301. 13 2.529 7.494 110228 0.61502

03/17/87- 3 301.21 20.883 21.326 314199 0.60904 03/17/87- 4 301.22 20.934 21.338 314435 0.60863 03/17/87- 5 301.27 20.882 21.316 314446 0.60876 03/17/87- 6 301.28 20.636 21.197 312758 0.60896

03/17/87- 7 301.31 68.779 38.561 569326 0.60681 03/17/87- 8 301.31 68. 797 38.558 569289 0.60669 03/17/87- 9 301.36 192.639 64 .390 951893 0.60546 03/17/87-10 301.39 192.632 64.384 952412 0.60542 03/18/87-11 301.03 2.517 7.468 109597 0.61431 03/18/87-12 301.06 2.510 7.464 109617 0.61478 03/18/87-13 301. 14 20.651 21.203 311919 0.60891 03/18/87-14 301. 17 20.763 21.247 312771 0.60854 03/18/87-15 301.20 21.047 21.396 315165 0.60865 03/18/87-16 301.22 21.053 21. 406 315448 .60886 03/18/87-17 301.26 69.279 38. 672 570365 0.60636 03/18/87-18 301.27 69.323 38.715 571118 0.60684 03/18/87-19 301.34 192.556 64.353 950944 0.60524 03/18/87-20 301.36 192.340 64 .339 951146 0.60546

47
Table 40. Measured and Calculated Quantities Using nitrogen Gas in the 4-Inch Orifice

Meter, 0.73 Beta Ratio, 3.8 iim Roughness

Run ID

46072386- 2 46072386- 3 46072386- 4 46072386- 5 46072386- 6 46072386- 7 46072486- 1 46072486- 2 46072486- 3 46072486- 4 46072486- 5 46072486- 6 46073186- 1 46073186- 2 46073186- 3 46073186- 4 46073186- 5 46073186- 6

Table 41

Pipe Diameter = 10.366 era Orifice Diameter = 7.6177 cm

Pressure Te mperature Density

(kg/m3

) Dif Press Flow Rate Pipe c CY 2 (MPa) (K) (kPa) (kg/s) Reynolds No.

3. 7209 286. 89 44.04 5.809 2.3379 1593100 6036 0.6037

3. 7206 286.87 44.04 5.773 2.3339 1590500 6044 0.6046

3. 8311 287. 15 45.31 4 .347 2.0455 1391100 6019 0.6020

3 . 8304 287. 14 45.30 4.360 2.0515 1395200 6028 0.6029

3.9614 287.52 46. 78 2.416 1.5561 1055700 6045 0.6046 3.9615 287.56 46. 78 2.434 1.5648 1061500 6057 0.6057 3.9703 288.08 46.79 2.336 1. 5340 1039200 6060 0.6060 3.9679 287.79 46.81 2.319 1.5233 1032700 6038 0.6039 3.8556 287.42 45.55 4.276 2.0406 1386500 6039 0.6040 3.8560 287. 31 45 57 4.256 2.0318 13S0900 6024 0.6025

3.6757 286.67 43.54 6.299 2.4190 1650100 6032 0. 6033

3 .6754 286. 97 43.49 6.314 2.4137 1645300 6015 . 6016

3. 7684 288.94 44 .26 4.406 2.0421 1383800 6038 6040

3. 7706 288.81 44.30 4.398 2.0421 1384300 6040 0.6042 3.5701 288.50 41.99 6. 645 2.4421 1660500 6037 0.6038 3.5831 287.90 42.24 6.621 2.4357 1658300 6014 0.6015

3 . 8447 289.00 45.15 2.586 1.5791 1068900 6035 0.6036

3 .8535 288.97 45.25 2.618 1.5907 1076800 6035 0.6036

Measured and Calculated Quantities Using Water in the 4-Inch Orifice Meter, 0.73 Beta Ratio, 6.9 urn Roughness

p. pe Diameter = 10.37!i cm Orifice Di ame t er = 7 6177 cm

Run ID Temperature Dif Press Flow Rate Pipe C (K) (kPa) (kg/s) Reynolds Mo. 03/13/87-- 1 299.87 2.572 7.543 107761 .61436 03/13/87- 2 299.91 2.563 7. 526 107648 . 61404 03/13/87- 3 300.05 20. 772 21.268 305106 0.60953

03/13/87- 4 300.06 20.796 21.283 305395 0. 60962 03/13/87- 5 300. 15 20.765 21.270 305796 0.60971

03/13/87- 6 300. 16 20. 857 21.322 306601 0.60984 03/13/87- 7 300. 16 69. 110 38.708 556616 0.60820

03/13/87- 8 300. 17 69.422 38.803 558108 0.60833

03/13/87- 9 300.20 69.383 38.787 558239 0.60825

03/13/87- 10 300.22 69.056 38.699 557210 0.60831 03/13/87- 11 300.37 193.046 64 .618 933603 .60751 03/13/87- 12 300.41 193.085 64.630 934585 0.60757

03/16/87- 13 299.25 2.510 7.448 104955 0.61402

03/16/87- 14 299.25 2.520 7.464 105179 0.61405

03/16/87- 15 299.44 21.014 21.356 302266 0.60848

03/16/87- 16 299.44 21.339 21.529 304718 0.60873 03/16/87- 17 300.22 20.635 21. 166 304806 0.60864 03/16/87- 18 300.26 20. 795 21.256 306358 0.60885

03/16/87- 19 300.32 69.017 38.622 : 557377 0.60727

03/16/87- 20 300133 68.917 38.576 • 556826 0.60697

03/16/87- 21 300; 42 193.242 64.576 933947 1 0.60681

03/16/87- 22 300:43 193.714 64.655 935283 ; 0.60681

Table 42. Measured and Calculated Quantities Using Ritrogen Gas in the 4 -Inch Orifice

Meter, 0.73 Beta Ratio, 6.9 jut Roughness

Pipe 'Diameter = 10.378 cm Orifice Diameter = 7.6177 cm

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe c CY 2 (MPa) (K) (kg/m3

) (kPa) (kg/s) Reynolds No. 46072286- 1 3. 7047 287.44 43.75 5/750 2.3256 1580900 .6060 0.6061 46072286- 2 3. 7044 287.36 43.77 5.677 2.3127 1572500 .6064 0.6066 46072286- 3 3.9026 287.72 46.05 2.450 1.5651 1060800 6091 0.6092 46072286- 4 3.9017 287.58 46.07 2.482 1.5749 1067700 6089 0.6090 46072286- 5 3 .8105 287.24 45.04 4.351 2.0560 1396600 6071 0.6072 46072286- 6 3.8089 287.26 45.02 4.327 2.0508 1393000 6074 0.6075 46072586- 1 3.8897 288.22 45.81 4. 117 2.0226 1369300 6088 0.6089 46072586- 2 3.8895 287.78 45.89 4.075 2.0119 1363600 6082 0.6083 46072586- 3 3.9876 287.83 47.04 2.398 1.5649 1059300 6092 0.6092 46072586- 4 3.9871 287.80 47.04 2.407 1.5619 1057300 6069 0.6069 46072586- 5 3.6867 286.92 43.63 5.984 2.3781 1619000 6084 0.6085 46080586- 1 3.8302 287.84 45.17 4.320 2.0529 1392100 6074 0.6075 46080586- 2 3.8298 287.93 45.15 4.316 2.0479 1388500 6064 0.6065 46080586- 3 3.9250 288.28 46.22 2.487 1.5725 1064000 6063 0.6064 46080586- 4 3.9246 288. 19 46.23 2.483 1.5741 1065400 6074 0.6075 46080586- 5 3.6139 287.61 42.65 6.828 2.5085 1706400 6076 0.6077 46080586- 6 3.6136 287.16 42.72 6.706 2.4886 1694800 6077 0.6079

48

Isllfl HUBBUHH
297 99 298 01 298 04 298 16 298 17 298 18 298 23 298 23 298 24 299 26

299 29 299 32 299 43 299 46 299 47 299 46 299 47 299 48

Table 43. Measured and Calculated Quantities Using Water in the 6-Inch Orifice Meter, 0.49 Beta Ratio, 2.8 jib Roughness

Pipe Diameter ; 15.563 cm Orifice Diameter - 7.7026 cm

Temperature Dif Press Flow Rate Pipe C (K) CkPa) (kg/s) Reynolds No. 2.571 6.620 60406 0.60688

2.567 6.617 60410 0.60706

2.569 6.617 60451 0.60691

21.192 18.937 173456 0.60469

21.102 18.893 173134 0.60458

21.331 18.992 174079 0.60449

129.042 46.598 427581 0.60300

129.154 46.621 427790 0.60304

129.343 46.638 428038 0.60281

2.516 6.543 61447 0.60642

2.5-20 6.547 61528 0.60635

2.512 6.541 61513 0.60678

21.081 18.875 177920 0.60438

20.854 18.770 177053 0.60430 21.179 18.918 178485 0.60437

129.300 46.623 439772 0.60280

129.439 46.640 440025 0.60270

129.332 46.624 439972 0.60274

Measured and Calculated Quantities Using Hater in the 6-Inch Orifice Meter, 0.49 Beta Ratio, 5.1 jia Roughness

Pipe Diameter = 15.433 cm ' Orifice Diameter = 7.7026 cm

Temperature Dif Press Flow Rate Pipe C

(K) CkPa) (kg/s) Reynolds No. 298.82 2.544 6.585 61758 0.60625

298.83 2.540 6.581 61742 0.60631

299.15 21.086 18.912 178679 0.60482

299.18 21.066 18.902 178707 0.60480

299.20 128.984 46.650 441324 0.60321

299.21 129.277 46.699 441889 0.60317

299.94 2.535 6.579 63272 0.60680 299.98 2.535 6.577 63312 0.60672

300.11 20.974 18.856 182014 0.60470

300.12 21.088 18.910 182579 0.60482

300.14 128.879 46.613 450231 0.60304

300.50 128.954 46.628 453970 0.60309

Measured and Calculated Quantities Using Water in the 6- Inch Orifice Meter, 0.49 Beta Ratio, 8.9 pa Roughness

Run ID

02/18/87- 1 02/18/87- 2 02/18/87- 3 02/18/87- 4 02/18/87- 5 02/18/87- 6 02/18/87- 7 02/18/87- a 02/18/87- 9 02/18/87- 10 02/18/87- 11 02/18/87- 12 02/18/87- 13 02/18/87- 14 02/18/87- 15 02/18/87- 16 02/18/87- 17 02/18/87- 18

Table 44. Mc as

Run ID

02/24/87- 1 02/24/87- 2 02/24/87- 5 02/24/87- 6 02/24/87- 7 02/24/87- 8 02/25/87- 10 02/25/87- 11 02/25/87- 13 02/25/87- 14 02/25/87- 15 02/25/87- 16

Table 45. M« as

Fipe Diameter = 15.573 cm Orifice Diameter = 7 7026 cm

Run ID Temperature Dif Press Flow Rate Pipe C (K) (kPa) (kg/s) Reynolds No. 02/27/87- 1 301.21 2.497 6.521 64423 0.60684 02/27/87- 2 301.25 2.490 6.513 64399 0.60705 02/27/87- 7 301. 42 20.913 18.797 186564 0.60449 02/27/87- 8 301. 44 20.895 18.797 186647 0.60476 02/27/87-11 301.68 128. 523 46. 510 464159 . 60335 02/27/87-12 301.68 128.547 46.521 464270 . 60344 03/02/87-13 300. 76 2.495 6.512 63703 0.60618 03/02/87-14 300. 80 2.492 6. 507 63710 0. 60617 03/02/87-17 300.99 21.058 18.858 185430 0. 60433 03/02/87-18 301. 02 20.960 18.822 185198 0.60459 03/02/87-21 301.21 128.443 46. 484 459212 0.60317 03/02/87-22 301.22 128.417 46.483 459299 0.60322

49
Table 46. Measured and Calculated Quantities Using Air in the 6-Inch Orifice Meter,

0.57 Beta Ratio, 2.8 urn Roughness

Run ID

11/13/87- 1 11/13/87- 2 11/13/87- 3 11/13/87- 4 11/13/87- 5 11/13/87- 6 11/13/87- 7 11/25/87- 1 11/25/87- 2 11/25/87- 3 11/25/87- 4 11/25/87- 5 11/25/87- 6

Table 47

Pipe Di ameter = 15.563 cm Orifice Diameter = 8.7808 cm

Pressure Temperature Density Dif Press Flow Rate Pipe c (MPa) (K) (kg/m 3

) (kPa) (kg/s) Reynolds No.

3. 5291 286.32 43. 47 2. 473 1. 7953 825000 6064

3. 5321 281. 76 44 .29 17 . 324 4 . 7868 2227000 6048 3.5293 278.04 44 . 92 47.989 8. 0322 3776000 6045 3.5287 276.93 45.11 48.005 8. 0508 3797000 6046

3 . 5288 277 .09 45.08 17.078 4 .7890 2257000 6042

3 . 5310 278.65 44 , 84 2.561 1.8520 869000 6055

3 . 5299 278. 98 44 . 76 2.557 1. 8493 867000 6056

3 . 5286 273. 43 45. 75 50. 973 8.3588 3982000 6048 3.5275 270 . 48 46.29 92. 174 11.3271 5442000 6045 3.5277 268.43 46.69 149.168 14.5159 7016000 6045 3.5284 267 . 32 46.93 149.292 14.5571 7060000 6044

3. 5280 266.04 47 . 17 93. 142 11.4868 5591000 6042 3.5282 265.65 47 .25 47.901 8.2195 4006000 6039

Measured and Calculated Quantities Using Air in the 6-Inch Orifice Meter,

0.57 Beta Ratio, 5.1 iim Roughness

Run ID

11/16/87- 1 11/16/87- 2 11/16/87- 3 11/16/87- 4 11/16/87- 5 11/16/87- 6 11/16/87- 7 11/25/87- 1 11/25/87- 2 11/25/87- 3 11/25/87- 4 11/25/87- 5

Table 48.

Pipe Diamet er =* 15.433 cm Orifice Diameter = 8 . 7808 cm

Pressure Temperature Density

(kg/ra 3

) Dif Press Flow Rate Pipe c (MPa) (K) (kPa) (kg/s) Reynolds No

.

3. 5286 280 . 15 44.53 2. 474 1. 8166 856000 6052

3 . 5265 275.87 45. 27 18. 168 4 . 9614 2367000 6044

3. 5278 271.76 46. 05 46. 549 8.0318 3877000 6051

3. 5284 270 . 65 46.28 46.535 8. 0476 3897000 6050

3. 5284 270 .43 46.33 17 .828 4 . 9668 2407000 6040

3 .5274 272.48 45.92 2.398 1. 8148 874000 6049

3 . 5282 273.32 45.76 2.399 1. 8116 871000 6047 3.5295 270 . 98 46. 13 102.422 11. 9826 5796000 6056

3 . 5289 268. 48 46.71 149.836 14 .6007 7115000 6054

3. 5291 267 .21 46.97 149.877 14 . 6411 7162000 6054

3 . 5295 265.98 47.21 93. 103 11. 5267 5659000 6051 3.5280 265.71 47.24 41. 418 7 . 6644 3766000 6048

Measured and Calculated Quantities Using Air in the 6-Inch Orifice Meter,

0.57 Beta Ratio, 8 . 9 iim Roughness

Pipe Di ameter = 15.573 cm Orifice Diameter = 8 . 7808 cm

Run ID Pressure Temperature Density

(kg/m 3

) Dif Press Flow Rate Pipe c (MPa) (K) (kPa) (kg/s) Reynolds No

.

11/16/87- 1 3.5281 285. 15 43.67 2.385 1. 7667 814000 6066 11/16/87- 2 3 .5280 280. 54 44.45 18.085 4 . 9142 2293000 6067 11/16/87- 3 3 .5279 275. 82 45. 30 46. 598 7.9791 3773000 6070 11/16/87- 4 3 .5284 274 . 15 45.62 46.604 8.0059 3803000 6069 11/16/87- 5 3 . 5280 273. 71 45. 70 18.091 4 .9750 2367000 6059 11/16/87- 6 3.5278 275. 09 45. 43 2. 627 1.8847 893000 6045 11/25/87- 1 3.5291 273.65 45. 72 48.625 8. 1951 3899000 6075 11/25/87- 2 3. 5286 270. 54 46.29 92.483 11. 3956 5470000 6072 11/25/87- 3 3. 5279 268.43 46. 69 148. 535 14 .5517 7028000 6074 11/25/87- 4 3. 5294 267. 15 46.97 148. 608 15. 0461 7075000 6072 11/25/87- 5 3.5288 265.93 47.21 92.192 11.4804 5587000 6069

Table 49. Measured and Calculated Quantities Using Water in the 6-Inch Orifice Meter, 0.66 Beta Ratio, 2.8 m" Roughness

Pipe Diameter = 15.563 cm Orifice Diameter = 10.3215 cm

Run ID Temperature Dif Press Flow Rate Pipe c (K) (kPa) (kg/s) Reynolds No. 02/17/87- 1 297 .90 2.550 12.854 117061 61032 02/17/87- 2 297. 45 2.554 12.852 115826 60981 02/17/87- 3 297 .47 2. 553 12.857 115922 61018

02/17/87- 4 297. 51 21.141 36.766 331869 60630 02/17/87- 5 297 . 51 21. 136 36.765 331857 60636

2/17/87- 6 297 . 52 21. 131 36.752 331812 60622 02/17/87- 7 297.75 162. 444 101. 450 920640 60356

02/17/87- 8 297 . 83 162.207 101 .349 921367 60341 02/17/87- 9 297 . 90 162. 087 101.322 922749 60347 02/18/87- 13 298. 59 2. 517 12. 769 118132 61043 02/18/87- 14 298.61 2.522 12.794 118413 61093 02/18/87- 15 298.62 2. 515 12. 762 118141 61031

02/18/87- 19 298. 70 21.656 37.210 345058 60636 02/18/87- 20 298. 71 21.690 37 .245 345456 60645 02/18/87- 21 298.73 21. 727 37.256 345713 60612

02/18/87- 22 298. 98 163.982 101. 875 950742 60332 02/18/87- 23 299. 05 163. 720 101.757 951090 60311 02/18/87- 24 299. 12 164 . 194 101 . 935 954205 60329

50
Table 50. Measured and Calculated Quantities Using Air in the 6-Inch Orifice Meter, 0.66 Beta Ratio, 2.8 ym Roughness

Pipe Diameter = 15.563 cm Orifice Diameter = 10.3215 cm

Run ID Pressure Temperature Density

(kg/m3

) Dif Press Flow Rate Pipe c (MPa) (K) (kPa) (kg/s) Reynolds No. 11/13/87- 1 3.5295 278.26 AA.88 2. A56 2.6376 1239000 .6035 11/13/87- 2 3. 5288 27A.0A A5.6A 22.3A6 7 . 9950 3802000 .6008 11/13/87- 3 3. 5290 270.37 A6. 3A 56.858 12.8643 6182000 .6005 11/13/87- A 3.5303 269.65 A6.50 56.572 12.8553 6192000 .6006 11/13/87- 5 3.5305 269.76 A6. A7 22.396 8.0703 3885000 . 600A 11/13/87- 6 3.5305 271.71 A6. 10 2.628 2.7538 1318000 .6011 11/30/87- 1 3. 5266 264.65 A7 .A3 121. 137 19.0114 9293000 .5991 11/30/87- 2 3.5169 258.82 A8.52 188.655 2A. 1588 12021000 .6011 11/30/87- 3 3. 5282 257. 0A A9. 06 189.216 2A . 3262 12171000 .6011 11/30/87- A 3.5228 25A.82 A9. A7 118.629 19.2A32 969AO00 6002 11/30/87- 5 3.5298 253.65 A9.83 5A.979 13. 1106 6630000 6005

Table 51. Measured and Calculated Quantities Using Hater in the 6-Inch Orifice Meter, 0.66 Beta Ratio, 5.1 iim Roughness

Pipe Diameter TM 15

.

A33 cm Orifice 1 Diameter 10 3215 cm

Run ID Temperature Dif Press Flow Rate Pipe C (K) (kPa) (kg/s) Reynolds No. 02/20/87 -1 300. A3 2.519 12.833 12A751 0.61072

02/20/87 -2 300. A5 2.520 12.8A1 12A887 .61103 02/20/87 -3 300.52 21. 163 36.960 359995 .60689 02/20/87 -A 300. 5A 21.269 37.0A6 360990 0.60679 02/20/87 -5 300.69 163.509 102.235 999618 0.60396 02/20/87 -6 300.77 162.935 102.030 999311 0.60381 02/2A/87 -9 299. A5 2.517 12.838 122117 0.61122 02/2A/87-10 299. A7 2.51A 12.836 122151 0.611A9 02/2A/87-11 299.52 20.719 36.558 3A8269 0.60663 02/2A/87-12 299.53 20.727 36.566 3A8A17 0.6066A 02/2A/87-15 300.08 162.827 102. 035 98A283 0.60A00 02/2A/87-16 300. 15 162. 8A7 102.083 98622A 0.60A2A

e 52. Measured and Calculated Quantities Using Air in the 6-Inch Orifice Meter

Pipe Diame ter = 15. A33 cm Orifice Diameter = 10.3215 cm

Run ID Pressure Temperature Density

(kg/m3

) Dif Press Flow Rate Pipe c (MPa) (K) (kPa) (kg/s) Reynolds No. 11/16/87- 1 3.5282 278. 59 AA.80 2. A86 2.6603 1259000 .6029 11/16/87- 2 3.5282 273. 0A A5.83 21.668 7.9A83 3822000 . 6029 11/16/87- 3 3.5276 269.26 A6.53 57.551 13.0671 635A000 . 6025 11/16/87- A 3.5279 267.76 A6. 8A 57.591 13. 1075 6A01000 .6023 11/16/87- 5 3.5278 267. 0A A6.97 21.853 8.0730 3951000 602A 11/16/87- 6 3.5277 269.71 A6. A5 2. A17 2.6685 1296000 .6026 12/01/87- 1 3.5227 270.37 A6.25 115.825 18.5025 8967000 601A 12/01/87- 2 3.5271 26A.15 A7. 5A 185.607 23.8576 11778000 6022 12/01/87- 3 3.529A 261. A8 A8. 12 185. 70A 2A .0032 119A5000 6021 12/01/87- A 3.52A6 259.09 A8.57 111.001 18.5129 9280000 0. 6003 12/01/87- 5 3.5273 258.15 A8.81 56.89A 13.2739 667A000 6013

Table 53. Measured and Calculated Quantities Using Water in the 6- Inch Orifice Meter, 0.66 Beta Ratio, 8.9 pa Roughness

Pipe Diameter - 15.573 cm Orifice Diameter - 10.3215 cm

Temperature Dif Press Flow Rate Pipe C (K) (kPa) (kg/s) Reynolds No. 2.513 12.7AA 1258A3 0.60999

2.503 12.731 1257A6 0.61058

20.996 36.660 363160 0.60708

20.945 36.619 362758 0.60715

162. AA3 101.730 1011822 0.60566

162.102 101.631 1012335 0.60571

2.505 12.732 1230A6 0.61031

2.502 12.726 123036 0.610A3

20.887 36.579 35A11A 0.6072A

20.911 36.575 35A151 0.6068A

163.367 102.005 993218 0.60551 03/02/87-18 300. 6A 163. 87A 102.166 996918 0.6055A

Run ID

02/26/87- 1 02/26/87- 2 02/26/87- 5 02/26/87- 6 02/26/87- 7 02/26/87- 8 03/02/87-•11 03/02/87- 12 03/02/87- 13 03/02/87- 14 03/02/87- 17

301 .19 301 .20 301 .34 301 34 301 .52 301 .59 300 .21 300 .23 300 .28 300 .29 300 . 55 300 ,6A

51
Table 54. Measured and Calculated Quantities Using Air in the 6-Inch Orifice Meter, 0.66 Beta Ratio, 8.9 fus Roughness

Run ID

11/16/87- 1 11/16/87- 2 11/16/87- 3 11/16/87- 4 11/16/87- 5 11/16/87- 6 12/01/87- 1 12/01/87- 2 12/01/87- 3 12/01/87- 4 12/01/87- 5

Table 55

Pipe Diameter = 15.573 cm Orifice Diair eter = 10. 3215 cm

Pressure Temperature Density Dif Press Flow Rate Pipe c (MPa) (K) Ckg/m 3

) (kPa) (kg/s) Reynolds No. 3.5277 281.37 44 .31 2.416 2.6036 1212000 6046 3.5272 275.43 45.36 22.891 8. 1379 3852000 6062 3.5275 270. 76 46.25 58.147 13.1111 6290000 6059 3.5275 269.32 46.52 58.209 13. 1506 6336000 6056

3. 5275 269.48 46. 49 22.739 8.2000 3949000 6056 3.5277 273.37 45.75 2.600 2.7383 1304000 6033

3. 5259 270.65 46.25 113.431 18.3850 8823000 6066 3.5258 264.82 47.38 186.306 23.9597 11698000 6072 3.5256 262.54 47.85 186.425 24.0653 11830000 6068

3 .5264 261.09 48. 17 118.458 19.1520 9457000 6059 3.5265 261.26 48. 14 55.907 13. 1102 6470000 6059

Measured and Calculated Quantities Using Water in the 6-Inch Orifice Meter,

0.74 Beta Ratio, 2.8 jibi Roughness

Pipe Diameter = 15.563 cm Orifice Diameter = 11 5540 cm

Run ID Temperature Dif Press Flow Rate Pipe C (K) (kPa) (kg/s) Reynolds No. 02/13/87- 1 297.03 2.561 17. 319 154590 0. 60837 02/13/87- 2 297.06 2. 562 17.320 154702 .60839 02/13/87- 3 297 .08 2. 565 17.326 154825 0. 60818 02/13/87- 4 297. 12 7.225 28.927 258729 0.60505

02/13/87- 5 297 . 13 7.221 28.946 258952 0.60557 02/13/87- 6 297.15 7.221 28.942 259032 0.60552

02/13/87- 7 297. 16 21.042 49. 164 440123 0.60254 02/13/87- 8 297.17 21.000 49. 143 440027 0.60288 02/13/87- 9 297.17 20.948 49. 113 439855 0.60325 02/13/87-10 297.27 20.925 49.033 440131 0.60263 02/13/87-11 297.30 20.992 49.097 440999 0.60245 02/13/87-12 297.33 21.264 49.418 444186 0.60250 02/13/87-13 297.34 69.248 88.824 798549 0.60009 02/13/87-14 297.34 69.211 88.844 798729 0.60039 02/13/87-15 297.37 69.200 88.836 799195 0.60039 02/13/87-16 297.63 188.792 146. 450 1325465 0.59924 02/13/87-17 297.68 188.517 146.337 1325917 0.59922 02/13/87-18 297.73 188.562 146.362 1327621 0.59925 02/17/87-20 296. 46 2.557 17.290 152287 0.60779 02/17/87-21 296.99 2.499 17. 105 152541 0.60833 02/17/87-22 296.55 2.551 17.285 152594 0. 60841 02/17/87-23 296.60 20. 795 48.937 432500 0.60329 02/17/87-24 297.01 20. 796 48.923 436492 0.60311 02/17/87-25 296.61 20. 752 48.916 432410 0.60365 02/17/87-26 297.17 20. 615 48. 703 436095 0. 60305 02/17/87-27 296.81 20.608 48.686 432325 0.60291 02/17/87-28 296.84 20.631 48. 710 432830 0.60288 02/17/87-29 296.97 191.503 147 .456 1314414 0. 59903 02/17/87-30 297 . 03 191.015 147.326 1315029 0.59927 02/17/87-31 297. 10 192.080 147.758 1320960 0.59936

Table 56. Measured and Calculated Quantities Using Air in the 6- Inch Orifice Meter,

0.74 Beta Ratio, 2.8 iim Roughness

Pipe Diameter = 15.563 cm Orifice Diameter = 11. 5540 cm

Run ID Pressure Temperature Density

(kg/m 3

) Dif Press Flow Rate Pipe c (MPa) (K) (kPa) (kg/s) Reynolds No

.

11/13/87- 1 3 .5300 282.98 44.07 2. 808 3. 7444 1736000 5994 11/13/87- 2 3. 5286 276.54 45.17 22. 420 10.6653 5035000 5964 11/13/87- 3 3.5195 271.48 45.99 59.929 17.6085 8435000 5960 11/13/87- 4 3.5289 270. 15 46.37 60.156 17.7114 8517000 5959 11/13/87- 5 3.5292 269.93 46. 42 22.094 10.8567 5159000 5958 11/13/87- 6 3.5245 272.76 45. 83 1.837 3.0781 1469000 5977 11/30/87- 1 3.5230 266.48 47.01 114.770 24.6840 12000000 5957 11/30/87- 4 3.5279 254.93 49.51 119.271 25.7781 12982000 5948

52
Table 57. Measured and Calculated Quantities Dsing Hater in the 6-Inch Orifice Meter,

0.74 Beta Ratio, 5.1 iim Roughness

Pipe Diameter • 15.433 cm Orifice Diameter = 11 .5540 i :m

Run ID Temperature Dif Press Flow Rate Pipe C

(K) (kPa) (kg/s) Reynolds No. 02/19/87- 1 299.01 2.583 17.511 164937 . 60802 02/19/87- 2 299.04 2. 548 17 .398 163984 .60829 02/19/87- 4 299. 10 20.904 49.422 466431 . 60329 02/19/87- 5 299. 12 20 .937 49.485 467236 .60359 02/19/87- 6 299.20 189.397 147.911 1399302 . 59985 02/19/87- 7 299.26 189.047 147.834 1400401 .60010 02/20/87-10 299.56 2.533 17.399 165926 .61017 02/20/87-11 299.59 2.494 17.259 164695 .60995

02/20/87-1'. 299.61 20.693 49. 192 469639 .60357 02/20/87-15 299.63 20. 696 49.206 469974 .60370 02/20/87-16 300.22 189.943 148.207 1433990 .60025 02/20/87-17 300.29 188. 852 147 .806 1432570 .60036 02/25/87-32 300.24 2.542 17.376 168233 .60835 02/25/87-33 300.30 2.549 17.394 168621 .60809 02/25/87-3* 300.37 20. 885 49.376 479381 .60308 02/25/87-35 300.39 20.886 49.380 479632 .60313 02/25/87-38 300. 64 188.916 147.686 1442484 .59979 02/25/87-39 300. 70 188.830 147 .670 1444178 .59987

Table 58. Measured and Calculated Quantities Using Air in the 6-Inch Orifice Meter,

0.74 Beta Ratio, 5.1 iim Roughness

Pipe Diameter = 15.433 cm Orifice Diameter « 11. 5540 cm

Run ID Pressure Temperature Density

(kg/m 3

) Dif Press Flow Rate Pipe c (MPa) (K) (kPa) (kg/s) Reynolds No

.

11/16/87- 1 3.5285 280.15 44 . 53 2.431 3.5358 1666000 . 6006 11/16/87- 2 3.5285 273.87 45.67 20.848 10.4680 5022000 . 5993 11/16/87- 3 3.5273 268.82 46.61 58.953 17. 7808 8656000 . 5983 11/16/87- 4 3. 5282 267.04 46. 98 58.994 17.8434 8732000 . 5980 11/16/87- 5 3.5277 266.76 47.03 19.875 10.3537 5072000 . 5984 11/16/87- 6 3 .5281 270.65 46.28 2. 484 3.6269 1756000 .5982 12/08/87- 1 3.5266 264 .98 47.37 109.679 24 .4631 12046000 .5975 12/08/87- 4 3 .5273 256.59 49.14 111.547 25.0782 12670000 . 5963 12/08/87- 5 3.5274 255.59 49.37 65.186 19. 1947 9727000 .5970 12/09/87- 1 3. 5247 272.54 45. 88 107 . 471 23.8345 11479000 .5975 12/09/87- 4 3.5290 261. 65 48.09 108.852 24 .5180 12195000 .5967 12/09/87- 5 3.5281 260. 59 48. 30 65.593 19.0082 9485000 .5957

Table 59. Measured and Calculated Quantities Dsing Hater in the 6-Inch Orifice Meter,

0.74 Beta Ratio, 8.9 iim Roughness

Pipe Diameter = 15.573 cm Orifice Diameter = 11.5540 cm

Run ID Temperature Dif Press Flow Rate Pipe C CK) (kPa) (kg/s) Reynolds No. 02/26/87- 1 300.28 2.539 17.227 166769 .60829 02/26/87- 2 300.30 2.526 17. 181 166395 .60832 02/26/87- 5 300 .42 20 . 941 49. 163 477369 .60454 02/26/87- 6 300 . 41 20 . 998 49.223 477852 .60445 02/26/87- 7 300. 68 189.602 147.743 1442877 .60376 02/26/87- 8 300.74 189. 131 147.621 1443529 60403 02/27/87- 11 301.87 2.521 17 . 140 171776 .60760 02/27/87- 12 301.90 2. 529 17.177 172255 .60789 02/27/87- 13 301.91 20.892 49. 097 492459 60452 02/27/87- 14 301.90 20.981 49.200 493396 ,60452

02/27/87- 15 301. 99 189.021 147. 493 1481899 .60377 02/27/87- 16 302.07 189.353 147.659 1486073 .60393

Table 60. Measured and Calculated Quantities Dsing Air in the 6-Inch Orifice Meter,

0.74 Beta Ratio, 8.9/i» Roughness

Pipe Diameter = 15.573 cm Orifice Diameter = 11. 5540 cm

Run ID Pressure Temperature Density Dif Press Flow Rate Pipe c (MPa) (K) (kg/m 3

) (kPa) (kg/s) Reynolds No. 11/16/87- 1 3. 5280 278.65 44 .79 2.458 3.5462 1663000 .6022 11/16/87- 2 3.5273 271.32 46. 13 20.677 10. 4698 5015000 .6037 11/16/87- 3 3.5272 266.15 47. 14 59.012 17.8797 8695000 .6028 11/16/87- 4 3.5281 264 .15 47.56 59.047 17.9582 8785000 .6027 11/16/87- 5 3.5280 262.87 47. 82 20.349 10.5605 5186000 ,6031 11/16/87- 6 3 .5280 264 .87 47.41 2.403 3.5993 1757000 .6012 12/08/87- 1 3. 5283 264 . 15 47.56 107.537 24 .3597 11917000 .6045 12/08/87- 4 3 . 5293 257 .09 49.06 108.415 24 .8260 12411000 .6042 12/08/87- 5 3.5284 256.26 49.22 63.259 18.9574 9501000 .6042

53
Table 61. Measured and Calculated Quantities Using Hitrogen Gas in the 4-inch Orifice Meter, 0.43 Beta Ratio.

6.9 iim Roughness Honed to 1.3 iim Roughness for Two Pipe Diameters

Pipe Diame ter = 10. 426 cm Orifice Diameter = 4.4445 cm

Run ID Pressure Temperature Density

(kg/m 3

) Dif Press Flow Rate Pipe c CY 2 MPa (K) (kPa) (kg/s) Reynolds No. 43102688- 1 3.9882 288.66 46. 90 12.817 1.0441 702100 6033 0. 6037 43102688- 2 3 .9717 288.54 46. 72 12. 723 1.0370 697700 6025 . 6029 43102688- 3 3 . 8029 287. 82 44 . 85 46. 865 1.9486 1315800 6009 0. 6025 43102688- 4 3.8045 287.34 44. 95 47. 776 1.9679 1330400 6003 0.6019

Pipe Diameter - 10.426 cm Orifice Diameter = 5.7137 cm

Pressure Te uperature Density Dif Press Flow Rate Pipe c CY 2 MPa (K) (kg/m 3

) (kPa) (kg/s) Reynolds No

.

4 .0567 289.06 47 . 63 2. 744 .8318 558300 6053 . 6054

4 .0577 289.21 47 .62 2. 750 0. 8319 558200 6048 0. 6048 3.9654 288. 52 46.65 7.650 1.3737 924300 6048 . 6050

3 . 9528 288.39 46.53 7.573 1.3630 917500 6039 . 6041

3. 7686 287.36 44 . 53 21. 415 2.2357 1512000 6017 0. 6024

3. 7619 287.41 44.44 21. 199 2.2241 1504200 6022 .6029 3.8675 287.60 45.66 15.422 1.9205 1296500 6017 . 6021 3.8686 287. 70 45.65 15. 440 1.9243 1298800 6025 0.6030

Table 62. Measured and Calculated Quantities Using Ritrogen Gas in the 4-inch Orifice Meter, 0.55 Beta Ratio,

6.9 iim Roughness Honed to 1.3 pat Roughness for Two Pipe Diameters

Run ID

44102688- 1 44102688- 2 44102688- 3 44102688- 4 44102688- 1 44102688- 2 44102688- 3 44102688- 4

Table 63. Measured and Calculated Quantities Using Sitrogen Gas in the 4-inch Orifice Meter, 0.67 Beta Ratio,

6.9 iim Roughness Honed to 1.3 ftm Roughness for Two Pipe Diaaeters

Run ID

45101888- 1 45101888- 2 45101888- 3 45101888- 4 45101888- 5 45101888- 6 45101888- 7 45101888- 8 45101988- 1 45101988- 2 45101988- 3 45101988- 4 45101988- 5 45101988- 6 45101988- 7 45101988- 8

Table 64. Measured and Calculated Quantities Using Hitrogen Gas in the 4-inch Orifice Meter, 0.73 Beta Ratio,

6.9 pa Roughness Honed to 1.3 iam Roughness for Two Pipe Diaaeters

Pipe Diameter = 10.426 cm Orifice Diameter = 6 . 9840 cm

Pressure Te nperature Density

(kg/m 3

) Dif Press Flow Rate Pipe c CY 2 MPa (K) (kPa) (kg/s) Reynolds No

.

3.9693 288.31 46.74 2. 660 1. 3016 876100 6090 . 6091

3 .9640 288.29 46. 68 2.636 1.2960 872500 6095 0. 6096 3.9002 287.83 46. 00 4. 713 1.7187 1159200 6089 0.6090

3 .8999 287.84 46. 00 4. 699 1.7123 1154900 6075 0.6077 3.7452 287. 12 44 .29 8. 452 2.2491 1522400 6063 . 6065 3.7356 287. 48 44 . 11 8. 435 2.2374 1513300 6049 . 6051

3 . 8262 287 .29 45.22 6.615 2. 0089 1357900 6058 . 6060

3 .8159 287. 59 45. 05 6.600 2. 0003 1351300 6051 . 6052 3.9712 287. 79 46. 85 4 .688 1. 7239 1161800 6068 0.6069

3 . 9501 287. 92 46. 58 4 .686 1.7159 1156400 6058 0.6060

3. 7869 287 . 66 44 .69 8.381 2.2471 1518300 6055 0.6058

3. 7814 287 .23 44 . 70 8.340 2.2405 1515500 6052 0.6054

3. 8925 287. 63 45. 95 6. 400 1. 9911 1343700 6056 . 6058

3. 8799 287. 61 45. 80 6.366 1.9838 1339100 6060 . 6061 3.9974 288.24 47. 08 2. 792 1.3356 898900 6077 . 6078 3.9976 288.24 47. 08 2.801 1.3369 899800 6072 0.6073

Pipe Diameter - 10.368 cm Orifice

Dif Press

Diameter =

Flow Rate

7.6177 cm

Run ID Pressure 1 emperature Density Pipe c (kg/m 3

) CY 2 MPa (K) (kPa) (kg/s) Reynolds No. 46101888- 1 3.9625 288. 17 46.68 2.486 1.5705 1057600 .6048 0. 6049 46101888- 2 3 .9562 288.00 46. 64 2.473 1. 5661 1055200 6051 . 6051 46101888- 3 3.8909 287.80 45.90 3 . 640 1.8788 1267400 6031 .6032 46101888- 4 3. 8860 287. 76 45.85 3.624 1.8735 1264100 6030 . 6031 46101888- 5 3.7399 286.97 44.25 5.525 2.2666 1534900 6013 0.6015 46101888- 6 3. 7379 286. 94 44.23 5.514 2.2651 1534000 6017 0.6018 46101888- 7 3.8203 287.24 45.16 4.397 2.0498 1385800 6035 0.6036 46101888- 8 3.8240 287.66 45. 13 4.422 2.0545 1387600 6034 0. 6035 46101988- 1 3 .9680 288.40 46.71 2.511 1.5754 1060300 6036 0.6037 46101988- 2 3.9712 288. 18 46. 78 2.508 1.5754 1060800 6035 0.6035 46101988- 3 3 .7706 287.73 44.49 5.403 2.2507 1520700 6022 0.6024 46101988- 4 3.7821 287.15 44 . 72 5. 412 2.2574 1527200 6020 0.6021 46101988- 5 3.8520 287. 79 45.44 4.536 2. 0804 1404100 6012 0.6013 46101988- 6 3.8371 287.66 45.29 4 .516 2.0786 1403700 6030 0.6031 46101988- 7 3. 8946 287 .85 45. 94 3.636 1.8791 1267400 6032 0.6033 46101988- 8 3 .8971 287.91 45.95 3.630 1.8787 1267000 6035 0.6036

54
Table 65. Measured and Calculated Quantities Using Kitrogen Gas in the 4- inch Orifice Meter, 0.67 Beta Ratio,

6.9 iim Roughness Honed to 1.3 iim Roughness for Four Pipe Diaaeters

Run ID

45110188- 1 45110188- 2 45110188- 3 45110188- 4 45110188- 5 45110188- 6 45110188- 7 45110188- 8

Table 66. Measured and Calculated Quantities Using nitrogen Gas in the 4-inch Orifice Meter, 0.73 Beta Ratio, 6.9 |ia Roughness Honed to 1.3 Iim Roughness for Four Pipe Diameters

Pipe Dianleter = 10 . 426 era

Temperature Density

Orifice Diameter = 6.9840 cm

Pressure Dif Press Flow Rate Pipe c CY 2 MPa (K) (kg/m J

) (kPa) Ckg/s) Reynolds No

.

3.3258 287. 41 45.20 6. 069 1. 9212 1298300 .6050 . 6052

3. 8201 287. 42 45. 13 6.018 1. 9118 1292000 .6051 0.6053

3. 7012 287. 14 43. 76 8. 711 2.2664 1534800 .6054 0.6056

3. 7006 286. 79 43. 81 8.659 2.2593 1531300 6049 0. 6052

3. 9459 287.95 46. 52 2. 733 1.3115 883900 ,6067 0. 6068 3.9253 287 .97 46.28 2. 789 1.3222 891200 6072 . 6072

3. 8994 287.95 45.97 4. 123 1.6004 1079100 .6064 0.6065

3. 8845 287.64 45.85 4 . 100 1. 5914 1074000 6055 0.6056

Pipe Diameter = 10.426 cm Orifice Diameter = 7.6177 cm

Run ID Pressure Temperature Density

(kg/m 3

) Dif Press Flow Rate Pipe c CY 2 MPa (K) (kPa) (kg/s) Reynolds No. 46110188- 1 3.9051 287 . 79 46.07 2. 547 1. 5771 1063800 .6040 . 6041 46110188- 2 3. 9000 287 . 76 46.01 2. 536 1. 5749 1062400 .6049 0. 6049 46110188- 3 3. 7161 287.28 43.92 5.407 2.2391 1515600 6028 0. 6029 46110188- 4 3. 7072 286. 99 43 . 86 5. 359 2.2285 1509600 .6031 0. 6032 46110188- 5 3 . 8056 287. 53 44. 94 4.312 2. 0221 1366400 .6027 0. 6028 46110188- 6 3.7881 287.36 44 .76 4.313 2. 0205 1366100 ,6034 0.6035 46110188- 7 3.8440 287 . 43 45.41 3.531 1. 8375 1241400 ,6020 0. 6021 46110188- 8 3 . 8380 287. 61 45.31 3. 532 1.8371 1240700 .6026 0.6027

55
^^m
NBS-114A (rev. 2-eo

U.S. DEPT. OF COMM. BIBLIOGRAPHIC DATA

SHEET (See instructions)

1. PUBLICATION OR

REPORT NO. NIST/TN 1329

2. Performing Organ. Report No. 3. Publication Date July 1989

4. TITLE AND SUBTITLE

Effect of Pipe Roughness on Orifice Flow Measurement

5. AUTHOR(S)

J. A. Brennan, C.F. Sindt, S.E. McFaddin, and R.R. Wilson

6. PERFORMING ORGANIZATION (If joint or other than NBS, see instructions)

NATIONAL BUREAU OF STANDARDS

DEPARTMENT OF COMMERCE

WASHINGTON, D.C. 20234

7. Contract/Grant No. 5081-353-0422

503 1-27 1-1680_

8. Type of Report & Period Covered

9. SPONSORING ORGANIZATION NAME AND COMPLETE ADDRESS (Street. City. State, ZIP)

Gas Research Institute

8600 West Bryn Mawr Avenue

Chicago, Illinois 60631

10. SUPPLEMENTARY NOTES

J

Document describes a computer program; SF-185, FlPS Software Summary, is attached.

11. ABSTRACT (A 200-word or less factual summary of most significant information. If document includes a significant

bibliography or literature survey, mention it here) Flow measurement with orifice flowmeters is simple in concept and can be

accurate, but as has been demonstrated in flow measurement test facilities can

also result in large errors if any of the significant parameters are not

controlled. Many of these parameters are well known and particular care is

taken to ensure that they do not cause measurement errors . Others are more

subtle and not so easily detected or controlled. One such parameter is the

surface finish of the pipe immediately upstream of the orifice plate. Results

of an experimental investigation into the effects of this pipe roughness on the

orifice discharge coefficient are presented, along with a review of some of the

pertinent literature. Measurement errors of approximately 1 percent can result

from using meter tubes that are too rough but still within the specification of

the standards.

12. KEY WORDS (Six to twelve entries; alphabetical order; capitalize only proper names; and separate key words by semicolons)

air; experimental; flow measurement; gas; orifice discharge coefficient; orifice

meter; roughness; surface finish; water

13. AVAILABILITY

23 Unlimited For Official Distribution. Do Not Release to NTIS

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]] Order From National Technical Information Service (NTIS), Springfield, VA. 22161

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PRINTED PAGES

66

15. Price

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